Hdpe articles

ABSTRACT

This disclosure relates to manufactured articles containing ethylene interpolymers. Specifically, films, containers and lids comprising at least one layer of an ethylene interpolymer product, or a blend containing an ethylene interpolymer product, where the ethylene interpolymer product has: a Dilution Index (Y d ) greater than 0; total catalytic metal ≧3.0 ppm; ≧0.03 terminal vinyl unsaturations per 100 carbon atoms, and; optionally a Dimensionless Modulus (X d ) greater than 0. The ethylene interpolymer products have a melt index from about 0.4 to about 100 dg/minute, a density from about 0.950 to about 0.970 g/cm 3 , a polydispersity (M w /M n ) from about 2 to about 25 and a CDBI 50  from about 55% to about 97%. Further, the ethylene interpolymer products are a blend of at least two ethylene interpolymers; where one ethylene interpolymer is produced with a single-site catalyst formulation and at least one ethylene interpolymer is produced with a heterogeneous catalyst formulation.

FIELD

This disclosure relates to manufactured articles comprising at least one ethylene interpolymer product manufactured in a continuous solution polymerization process utilizing at least two reactors employing at least one single-site catalyst formulation and at least one heterogeneous catalyst formulation to produce manufactured articles having improved properties.

BACKGROUND

Ethylene interpolymer products are widely used in film and molding applications to produce a wide variety of manufactured articles. There is a need to improve the heat deflection temperature (HDT) of ethylene interpolymer products; such products with higher HDT are desired and valued in many applications. Non-limiting examples include: injection molding where a molded part maintains its dimensional stability at higher temperatures, i.e. the molded part has a higher upper use temperature and is functional over a wider temperature range. Further, higher heat deflection temperatures are also desirable in film applications, for example in the packaging of hot foods, or the cooking of foods within a film comprising a least one layer of an ethylene interpolymer product having a higher heat deflection temperature. There is also a need for ethylene interpolymer products having faster crystallization rates in many applications; a non-limiting example includes injection molding where more rapid crystallization allows parts to “set up” or harden more quickly, thus more parts can be produced per hour. There is also a need for ethylene interpolymer products having higher melt strength in many applications. Non-limiting examples include: the production of blown film where higher melt strength improves the stability of the blown film bubble and improved bubble stability allows the production of film at higher rates; higher melt strength is also desired in blow molding and thermoforming applications. Further, higher melt strength is desired in and foam applications where molten ethylene interpolymer products are foamed with chemical or physical blowing agents.

Herein, manufactured articles comprising ethylene interpolymers products having improved heat deflection temperature, faster crystallization rates and higher melt strengths are disclosed.

The ethylene interpolymer products disclosed were produced in a solution polymerization process, where catalyst components, solvent, monomers and hydrogen are fed under pressure to one or more reactors. For ethylene homo polymerization, or ethylene copolymerization, reactor temperatures can range from about 80° C. to about 300° C. while pressures generally range from about 3MPag to about 45 MPag and the ethylene interpolymer produced is dissolved in a solvent. The residence time of the solvent in the reactor is relatively short, for example, from about 1 second to about 20 minutes. The solution process can be operated under a wide range of process conditions that allow the production of a wide variety of ethylene interpolymers. Post reactor, the polymerization reaction is quenched to prevent further polymerization, by adding a catalyst deactivator, and passivated, by adding an acid scavenger. Once passivated, the polymer solution is forwarded to a polymer recovery operation where the ethylene interpolymer is separated from process solvent, unreacted residual ethylene and unreacted optional α-olefin(s).

SUMMARY OF DISCLOSURE

This Application claims priority to Canadian Patent Application No. CA 2,868,640, filed Oct. 21, 2014 and entitled “SOLUTION POLYMERIZATION PROCESS”.

Embodiment of this disclosure include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has a Dilution Index, Y_(d), greater than 0.

Embodiment of this disclosure include manufactured articles having at least one layer containing an ethylene interpolymer product comprising (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer has ≧0.03 terminal vinyl unsaturations per 100 carbon atoms.

Embodiment of this disclosure include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has ≧3 parts per million (ppm) of a total catalytic metal.

Further embodiment include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has a Dilution Index, Y_(d), greater than 0 and 0.03 terminal vinyl unsaturations per 100 carbon atoms or ≧3 parts per million (ppm) of a total catalytic metal or a Dimensionless Modulus, X_(d), >0.

Additional embodiment include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has ≧0.03 terminal vinyl unsaturations per 100 carbon atoms and ≧3 parts per million (ppm) of a total catalytic metal or a Dimensionless Modulus, X_(d), >0.

Embodiments include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has ≧3 parts per million (ppm) of a total catalytic metal and a Dimensionless Modulus, X_(d), >0.

Further embodiments include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has a Dilution Index, Y_(d), greater than 0 and ≧0.03 terminal vinyl unsaturations per 100 carbon atoms and ≧3 parts per million (ppm) of a total catalytic metal or a Dimensionless Modulus, X_(d), >0.

Additional embodiments include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has a Dimensionless Modulus, X_(d), >0 and ≧3 parts per million (ppm) of a total catalytic metal and a Dilution Index, Y_(d), greater than 0 or ≧0.03 terminal vinyl unsaturations per 100 carbon atoms

Embodiments also include manufactured articles having at least one layer containing an ethylene interpolymer product comprising: (i) a first ethylene interpolymer; (ii) a second ethylene interpolymer, and; (iii) optionally a third ethylene interpolymer; where the ethylene interpolymer product has a Dilution Index, Y_(d), greater than 0, a Dimensionless Modulus, X_(d), >0, ≧3 parts per million (ppm) of a total catalytic metal and ≧0.03 terminal vinyl unsaturations per 100 carbon atoms.

The ethylene interpolymer products disclosed here have a melt index from about 0.4 to about 100 dg/minute, a density from about 0.950 to about 0.970 g/cm³, a M_(w)/M_(n) from about 2 to about 25 and a CDBI₅₀ from about 55% to about 98%; where melt index is measured according to ASTM D1238 (2.16 kg load and 190° C.) and density is measured according to ASTM D792.

Further, the disclosed ethylene interpolymer products contain: (i) from about 15 to about 60 weight percent of a first ethylene interpolymer having a melt index from about 0.01 to about 200 dg/minute and a density from about 0.855 g/cm³ to about 0.975 g/cm³; (ii) from about 30 to about 85 weight percent of a second ethylene interpolymer having a melt index from about 0.3 to about 1000 dg/minute and a density from about 0.89 g/cm³ to about 0.975 g/cm³, and; (iii) optionally from about 0 to about 30 weight percent of a third ethylene interpolymer having a melt index from about 0.5 to about 2000 dg/minute and a density from about 0.89 to about 0.975 g/cm³; where weight percent is the weight of the first, second or third ethylene polymer divided by the weight of ethylene interpolymer product.

Embodiments of this disclosure include manufactured articles comprising one or more ethylene interpolymer product synthesized in a solution polymerization process containing from 0 to about 1 mole percent of one or more α-olefins.

Further, the first ethylene interpolymer is synthesized using a single-site catalyst formulation and the second ethylene interpolymer is synthesized using a first heterogeneous catalyst formulation. Embodiments of manufactured articles may contain ethylene interpolymers where the third ethylene interpolymer is synthesized using a first heterogeneous catalyst formulation or a second heterogeneous catalyst formulation.

The second ethylene interpolymer may be synthesized using a first in-line Ziegler Natta catalyst formulation or a first batch Ziegler-Natta catalyst formulation; optionally, the third ethylene interpolymer is synthesized using the first in-line Ziegler Natta catalyst formulation or the first batch Ziegler-Natta catalyst formulation. The optional third ethylene interpolymer may be synthesized using a second in-line Ziegler Natta catalyst formulation or a second batch Ziegler-Natta catalyst formulation.

Embodiments of this disclosure include manufactured articles where the ethylene interpolymer product has ≦1 part per million (ppm) of a metal A; where metal A originates from the single-site catalyst formulation; non-limiting examples of metal A include titanium, zirconium or hafnium.

Further embodiments include manufactured articles where the ethylene interpolymer product has a metal B and optionally a metal C; where the total amount of metal B and metal C is from about 3 to about 11 parts per million (ppm); where metal B originates from a first heterogeneous catalyst formulation and metal C originates form an optional second heterogeneous catalyst formation. Metals B and C are independently selected from the following non-limiting examples: titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, technetium, rhenium, iron, ruthenium or osmium. Metals B and C may be the same metal.

Additional embodiments of manufactured articles contain ethylene interpolymer products where the first ethylene interpolymer has a first M_(w)/M_(n), the second ethylene interpolymer has a second M_(w)/M_(n) and the optional third ethylene has a third M_(w)/M_(n); where the first M_(w)/M_(n) is lower than the second M_(w)/M_(n) and the optional third M_(w)/M_(n). Embodiments also include ethylene interpolymer products where the blending of the second ethylene interpolymer and the third ethylene interpolymer form an ethylene interpolymer blend having a fourth M_(w)/M_(n); where the fourth M_(w)/M_(n) is not broader than the second M_(w)/M_(n). Additional ethylene interpolymer product embodiments are characterized as having both the second M_(w)/M_(n) and the third M_(w)/M_(n) less than about 4.0.

Further, embodiments of manufactured articles also include ethylene interpolymer products where the first ethylene interpolymer has a first CDBI₅₀ from about 70 to about 98%, the second ethylene interpolymer has a second CDBI₅₀ from about 45 to about 98% and the optional third ethylene interpolymer has a third CDBI₅₀ from about 35 to about 98%. Other embodiments include ethylene interpolymer products where the first CDBI₅₀ is higher than the second CDBI₅₀; optionally the first CDBI₅₀ is higher than the third CDBI₅₀.

Embodiments include manufactured articles, e.g. films, containers and lids, where the ethylene interpolymer product has melt strength that is from 5% to 30% higher, relative to a comparative ethylene interpolymer synthesized using one or more single-site catalyst formulations.

Further embodiments include manufactured articles having a heat deflection temperature that is from 4° C. to 10° C. higher, relative to a control manufactured article having the same construction but the ethylene interpolymer product is replaced with a comparative ethylene interpolymer synthesized using one or more single-site catalyst formulations.

Embodiments include manufactured articles having a first half time of crystallization (t_(1/2)) that is at least 70% lower, relative to a control manufactured article having the same construction but the ethylene interpolymer product is replaced with a comparative ethylene interpolymer synthesized using one or more single-site catalyst formulations.

BRIEF DESCRIPTION OF FIGURES

The following Figures are presented for the purpose of illustrating selected embodiments of this disclosure; it being understood, that the embodiments shown do not limit this disclosure.

FIG. 1 illustrates the gel permeation chromatograms (GPC) of four ethylene interpolymer products, Examples 20-22 and 24, and Comparative Example 10.

FIG. 2 shows Accelerated Haul Off (AHO) melt strength, measured in centi-Newtons (cN), of Examples 20-24 (solid symbols) as a function of melt index (I₂ g/10 min, measured according to ASTM D1238) and Comparative Examples D1-D8 (open symbols).

FIG. 3 illustrates the influence of melt flow properties and nucleation on the density of Examples 20-24 (Nuc=Nucleated).

FIG. 4 plots half-time of crystallization (t_(1/2)) for Examples 20-24 relative to Comparative Example 10; all samples were un-nucleated.

FIG. 5 plots half-time of crystallization (t_(1/2)) for Examples 20-24 relative to Comparative Example 10; all samples contain 1200 ppm of nucleator.

FIG. 6 shows the heat deflection temperature of Examples 20-24 (un-nucleated and nucleated) relative to Comparative Example 10 (un-nucleated and nucleated).

FIG. 7 is a plot of Dilution Index (Y_(d)) (Y_(d) has dimensions of degrees (°)) and Dimensionless Modulus (X_(d)) for:

-   -   Comparative S (open triangle, Y_(d)=X_(d)=0) is an ethylene         interpolymer comprising an ethylene interpolymer synthesized         using an in-line Ziegler-Natta catalyst in a solution process         (rheological reference);     -   Examples 6, 101, 102, 103, 110, 115, 200, 201 (solid circle,         Y_(d)>0 and X_(d)<0) are ethylene interpolymer products as         described in this disclosure comprising a first ethylene         interpolymer synthesized using a single-site catalyst         formulation and a second ethylene interpolymer synthesized using         an in-line Ziegler-Natta catalyst formulation in a solution         process;     -   Examples 120, 130 and 131 (solid square, Y_(d)>0, X_(d)>0) are         ethylene interpolymer products as described in this disclosure;     -   Comparatives D and E (open diamond, Y_(d)<0, X_(d)>0) are         ethylene interpolymers comprising a first ethylene interpolymer         synthesized using a single-site catalyst formation and a second         ethylene interpolymer synthesized using a batch Ziegler-Natta         catalyst formulation in a solution process, and;     -   Comparative A (open square, Y_(d)>0 and X_(d)<0) is an ethylene         interpolymer comprising a first and second ethylene interpolymer         synthesized using a single-site catalyst formation in a solution         process.

FIG. 8 illustrates a typical Van Gurp Palmen (VGP) plot of phase angle [°] versus complex modulus [kPa].

FIG. 9 plots the Storage modulus (G′) and loss modulus (G″) showing the cross over frequency ω_(x) and the two decade shift in phase angle to reach ω_(c) (ω_(c)=0.01 ω_(x)).

FIG. 10 compares the amount of terminal vinyl unsaturations per 100 carbon atoms (terminal vinyl/100 C) in the ethylene interpolymer products of this disclosure (solid circles) with Comparatives B, C, E, E2, G, H, H2, I and J (open triangles).

FIG. 11 compares the amount of total catalytic metal (ppm) in the ethylene interpolymer products of this disclosure (solid circles) with Comparatives B, C, E, E2, G, H, H2, I and J (open triangles).

DEFINITION OF TERMS

Other than in the examples or where otherwise indicated, all numbers or expressions referring to quantities of ingredients, extrusion conditions, etc., used in the specification and claims are to be understood as modified in all instances by the term “about.” Accordingly, unless indicated to the contrary, the numerical parameters set forth in the following specification and attached claims are approximations that can vary depending upon the desired properties that the various embodiments desire to obtain. At the very least, and not as an attempt to limit the application of the doctrine of equivalents to the scope of the claims, each numerical parameter should at least be construed in light of the number of reported significant digits and by applying ordinary rounding techniques. The numerical values set forth in the specific examples are reported as precisely as possible. Any numerical values, however, inherently contain certain errors necessarily resulting from the standard deviation found in their respective testing measurements.

It should be understood that any numerical range recited herein is intended to include all sub-ranges subsumed therein. For example, a range of “1 to 10” is intended to include all sub-ranges between and including the recited minimum value of 1 and the recited maximum value of 10; that is, having a minimum value equal to or greater than 1 and a maximum value of equal to or less than 10. Because the disclosed numerical ranges are continuous, they include every value between the minimum and maximum values. Unless expressly indicated otherwise, the various numerical ranges specified in this application are approximations.

All compositional ranges expressed herein are limited in total to and do not exceed 100 percent (volume percent or weight percent) in practice. Where multiple components can be present in a composition, the sum of the maximum amounts of each component can exceed 100 percent, with the understanding that, and as those skilled in the art readily understand, that the amounts of the components actually used will conform to the maximum of 100 percent.

In order to form a more complete understanding of this disclosure the following terms are defined and should be used with the accompanying figures and the description of the various embodiments throughout.

The term “Dilution Index (Y_(d))” and “Dimensionless Modulus (X_(d))” are based on rheological measurements and are fully described in this disclosure.

As used herein, the term “monomer” refers to a small molecule that may chemically react and become chemically bonded with itself or other monomers to form a polymer.

As used herein, the term “α-olefin” is used to describe a monomer having a linear hydrocarbon chain containing from 3 to 20 carbon atoms having a double bond at one end of the chain.

As used herein, the term “ethylene polymer”, refers to macromolecules produced from ethylene monomers and optionally one or more additional monomers; regardless of the specific catalyst or specific process used to make the ethylene polymer. In the polyethylene art, the one or more additional monomers are called “comonomer(s)” and often include α-olefins. The term “homopolymer” refers to a polymer that contains only one type of monomer. Common ethylene polymers include high density polyethylene (HDPE), medium density polyethylene (MDPE), linear low density polyethylene (LLDPE), very low density polyethylene (VLDPE), ultralow density polyethylene (ULDPE), plastomer and elastomers. The term ethylene polymer also includes polymers produced in a high pressure polymerization processes; non-limiting examples include low density polyethylene (LDPE), ethylene vinyl acetate copolymers (EVA), ethylene alkyl acrylate copolymers, ethylene acrylic acid copolymers and metal salts of ethylene acrylic acid (commonly referred to as ionomers). The term ethylene polymer also includes block copolymers which may include 2 to 4 comonomers. The term ethylene polymer also includes combinations of, or blends of, the ethylene polymers described above.

The term “ethylene interpolymer” refers to a subset of polymers within the “ethylene polymer” group that excludes polymers produced in high pressure polymerization processes; non-limiting examples of polymers produced in high pressure processes include LDPE and EVA (the latter is a copolymer of ethylene and vinyl acetate).

The term “heterogeneous ethylene interpolymers” refers to a subset of polymers in the ethylene interpolymer group that are produced using a heterogeneous catalyst formulation; non-limiting examples of which include Ziegler-Natta or chromium catalysts.

The term “homogeneous ethylene interpolymer” refers to a subset of polymers in the ethylene interpolymer group that are produced using metallocene or single-site catalysts. Typically, homogeneous ethylene interpolymers have narrow molecular weight distributions, for example gel permeation chromatography (GPC) M_(w)/M_(n) values of less than 2.8; M_(w) and M_(n) refer to weight and number average molecular weights, respectively. In contrast, the M_(w)/M_(n) of heterogeneous ethylene interpolymers are typically greater than the M_(w)/M_(n) of homogeneous ethylene interpolymers. In general, homogeneous ethylene interpolymers also have a narrow comonomer distribution, i.e. each macromolecule within the molecular weight distribution has a similar comonomer content. Frequently, the composition distribution breadth index “CDBI” is used to quantify how the comonomer is distributed within an ethylene interpolymer, as well as to differentiate ethylene interpolymers produced with different catalysts or processes. The “CDBI₅₀” is defined as the percent of ethylene interpolymer whose composition is within 50% of the median comonomer composition; this definition is consistent with that described in U.S. Pat. No. 5,206,075 assigned to Exxon Chemical Patents Inc. The CDBI₅₀ of an ethylene interpolymer can be calculated from TREF curves (Temperature Rising Elution Fractionation); the TREE method is described in Wild, et al., J. Polym. Sci., Part B, Polym. Phys., Vol. 20 (3), pages 441-455. Typically the CDBI₅₀ of homogeneous ethylene interpolymers are greater than about 70%. In contrast, the CDBI₅₀ of α-olefin containing heterogeneous ethylene interpolymers are generally lower than the CDBI₅₀ of homogeneous ethylene interpolymers.

It is well known to those skilled in the art, that homogeneous ethylene interpolymers are frequently further subdivided into “linear homogeneous ethylene interpolymers” and “substantially linear homogeneous ethylene interpolymers”. These two subgroups differ in the amount of long chain branching: more specifically, linear homogeneous ethylene interpolymers have less than about 0.01 long chain branches per 1000 carbon atoms; while substantially linear ethylene interpolymers have greater than about 0.01 to about 3.0 long chain branches per 1000 carbon atoms. A long chain branch is macromolecular in nature, i.e. similar in length to the macromolecule that the long chain branch is attached to. Hereafter, in this disclosure, the term “homogeneous ethylene interpolymer” refers to both linear homogeneous ethylene interpolymers and substantially linear homogeneous ethylene interpolymers.

Herein, the term “polyolefin” includes ethylene polymers and propylene polymers; non-limiting examples of propylene polymers include isotactic, syndiotactic and atactic propylene homopolymers, random propylene copolymers containing at least one comonomer and impact polypropylene copolymers or heterophasic polypropylene copolymers.

The term “thermoplastic” refers to a polymer that becomes liquid when heated, will flow under pressure and solidify when cooled. Thermoplastic polymers include ethylene polymers as well as other polymers commonly used in the plastic industry; non-limiting examples of other polymers commonly used in film applications include barrier resins (EVOH), tie resins, polyethylene terephthalate (PET), polyamides and the like.

As used herein the term “monolayer film” refers to a film containing a single layer of one or more thermoplastics.

As used herein, the terms “hydrocarbyl”, “hydrocarbyl radical” or “hydrocarbyl group” refers to linear or cyclic, aliphatic, olefinic, acetylenic and aryl (aromatic) radicals comprising hydrogen and carbon that are deficient by one hydrogen.

As used herein, an “alkyl radical” includes linear, branched and cyclic paraffin radicals that are deficient by one hydrogen radical; non-limiting examples include methyl (—CH₃) and ethyl (—CH₂CH₃) radicals. The term “alkenyl radical” refers to linear, branched and cyclic hydrocarbons containing at least one carbon-carbon double bond that is deficient by one hydrogen radical.

Herein the term “R1” and its superscript form “^(R1)” refers to a first reactor in a continuous solution polymerization process; it being understood that R1 is distinctly different from the symbol R¹; the latter is used in chemical formula, e.g. representing a hydrocarbyl group. Similarly, the term “R2” and it's superscript form “^(R2)” refers to a second reactor, and; the term “R3” and it's superscript form “^(R3)” refers to a third reactor.

DETAILED DESCRIPTION Catalysts

Organometallic catalyst formulations that are efficient in polymerizing olefins are well known in the art. In the embodiments disclosed herein, at least two catalyst formulations are employed in a continuous solution polymerization process. One of the catalyst formulations is a single-site catalyst formulation that produces a first ethylene interpolymer. The other catalyst formulation is a heterogeneous catalyst formulation that produces a second ethylene interpolymer. Optionally a third ethylene interpolymer is produced using the heterogeneous catalyst formulation that was used to produce the second ethylene interpolymer, or a different heterogeneous catalyst formulation may be used to produce the third ethylene interpolymer. In the continuous solution process, the at least one homogeneous ethylene interpolymer and the at least one heterogeneous ethylene interpolymer are solution blended and an ethylene interpolymer product is produced.

Single Site Catalyst Formulation

The catalyst components which make up the single site catalyst formulation are not particularly limited, i.e. a wide variety of catalyst components can be used. One non-limiting embodiment of a single site catalyst formulation comprises the following three or four components: a bulky ligand-metal complex; an alumoxane co-catalyst; an ionic activator and optionally a hindered phenol. In Table 2A of this disclosure: “(i)” refers to the amount of “component (i)”, i.e. the bulky ligand-metal complex added to R1; “(ii)” refers to “component (ii)”, i.e. the alumoxane co-catalyst; “(iii)” refers to “component (iii)” i.e. the ionic activator, and; “(iv)” refers to “component (iv)”, i.e. the optional hindered phenol.

Non-limiting examples of component (i) are represented by formula (I):

(L^(A))_(a)M(PI)_(b)(Q)_(n)  (I)

wherein (L^(A)) represents a bulky ligand; M represents a metal atom; PI represents a phosphinimine ligand; Q represents a leaving group; a is 0 or 1; b is 1 or 2; (a+b)=2; n is 1 or 2, and; the sum of (a+b+n) equals the valance of the metal M.

Non-limiting examples of the bulky ligand LA in formula (I) include unsubstituted or substituted cyclopentadienyl ligands or cyclopentadienyl-type ligands, heteroatom substituted and/or heteroatom containing cyclopentadienyl-type ligands. Additional non-limiting examples include, cyclopentaphenanthreneyl ligands, unsubstituted or substituted indenyl ligands, benzindenyl ligands, unsubstituted or substituted fluorenyl ligands, octahydrofluorenyl ligands, cyclooctatetraendiyl ligands, cyclopentacyclododecene ligands, azenyl ligands, azulene ligands, pentalene ligands, phosphoyl ligands, phosphinimine, pyrrolyl ligands, pyrozolyl ligands, carbazolyl ligands, borabenzene ligands and the like, including hydrogenated versions thereof, for example tetrahydroindenyl ligands. In other embodiments, L^(A) may be any other ligand structure capable of η-bonding to the metal M, such embodiments include both η³-bonding and η⁵-bonding to the metal M. In other embodiments, L^(A) may comprise one or more heteroatoms, for example, nitrogen, silicon, boron, germanium, sulfur and phosphorous, in combination with carbon atoms to form an open, acyclic, or a fused ring, or ring system, for example, a heterocyclopentadienyl ancillary ligand. Other non-limiting embodiments for L^(A) include bulky amides, phosphides, alkoxides, aryloxides, imides, carbolides, borollides, porphyrins, phthalocyanines, corrins and other polyazomacrocycles.

Non-limiting examples of metal M in formula (I) include Group 4 metals, titanium, zirconium and hafnium.

The phosphinimine ligand, PI, is defined by formula (II):

(R^(p))₃P=N—  (II)

wherein the R^(p) groups are independently selected from: a hydrogen atom; a halogen atom; C₁₋₂₀ hydrocarbyl radicals which are unsubstituted or substituted with one or more halogen atom(s); a C₁₋₈ alkoxy radical; a C₆₋₁₀ aryl radical; a C₆₋₁₀ aryloxy radical; an amido radical; a silyl radical of formula —Si(R^(s))₃, wherein the R^(s) groups are independently selected from, a hydrogen atom, a C₁₋₈ alkyl or alkoxy radical, a C₆₋₁₀ aryl radical, a C₆₋₁₀ aryloxy radical, or a germanyl radical of formula —Ge(R^(G))₃, wherein the R^(G) groups are defined as R^(s) is defined in this paragraph.

The leaving group Q is any ligand that can be abstracted from formula (I) forming a catalyst species capable of polymerizing one or more olefin(s). An equivalent term for Q is an “activatable ligand”, i.e. equivalent to the term “leaving group”. In some embodiments, Q is a monoanionic labile ligand having a sigma bond to M. Depending on the oxidation state of the metal, the value for n is 1 or 2 such that formula (I) represents a neutral bulky ligand-metal complex. Non-limiting examples of Q ligands include a hydrogen atom, halogens, C₁₋₂₀ hydrocarbyl radicals, C₁₋₂₀ alkoxy radicals, C₅₋₁₀ aryl oxide radicals; these radicals may be linear, branched or cyclic or further substituted by halogen atoms, C₁₋₁₀ alkyl radicals, C₁₋₁₀ alkoxy radicals, C₆₋₁₀ arly or aryloxy radicals. Further non-limiting examples of Q ligands include weak bases such as amines, phosphines, ethers, carboxylates, dienes, hydrocarbyl radicals having from 1 to 20 carbon atoms. In another embodiment, two Q ligands may form part of a fused ring or ring system.

Further embodiments of component (i) of the single site catalyst formulation include structural, optical or enantiomeric isomers (meso and racemic isomers) and mixtures thereof of the bulky ligand-metal complexes described in formula (I) above.

The second single site catalyst component, component (ii), is an alumoxane co-catalyst that activates component (i) to a cationic complex. An equivalent term for “alumoxane” is “aluminoxane”; although the exact structure of this co-catalyst is uncertain, subject matter experts generally agree that it is an oligomeric species that contain repeating units of the general formula (III):

(R)₂AlO—(Al(R)—O)_(n)—Al(R)₂  (III)

where the R groups may be the same or different linear, branched or cyclic hydrocarbyl radicals containing 1 to 20 carbon atoms and n is from 0 to about 50. A non-limiting example of an alumoxane is methyl aluminoxane (or MAO) wherein each R group in formula (III) is a methyl radical.

The third catalyst component (iii) of the single site catalyst formation is an ionic activator. In general, ionic activators are comprised of a cation and a bulky anion; wherein the latter is substantially non-coordinating. Non-limiting examples of ionic activators are boron ionic activators that are four coordinate with four ligands bonded to the boron atom. Non-limiting examples of boron ionic activators include the following formulas (IV) and (V) shown below;

[R⁵]⁺[B(R⁷)₄]⁻  (IV)

where B represents a boron atom, R⁵ is an aromatic hydrocarbyl (e.g. triphenyl methyl cation) and each R⁷ is independently selected from phenyl radicals which are unsubstituted or substituted with from 3 to 5 substituents selected from fluorine atoms, C₁₋₄ alkyl or alkoxy radicals which are unsubstituted or substituted by fluorine atoms; and a silyl radical of formula —Si(R⁹)₃, where each R⁹ is independently selected from hydrogen atoms and C₁₋₄ alkyl radicals, and; compounds of formula (V);

[(R⁸)_(t)ZH]⁺[B(R⁷)₄]⁻  (V)

where B is a boron atom, H is a hydrogen atom, Z is a nitrogen or phosphorus atom, t is 2 or 3 and R⁸ is selected from C₁₋₈ alkyl radicals, phenyl radicals which are unsubstituted or substituted by up to three C₁₋₄ alkyl radicals, or one R⁸ taken together with the nitrogen atom may form an anilinium radical and R⁷ is as defined above in formula (IV).

In both formula (IV) and (V), a non-limiting example of R⁷ is a pentafluorophenyl radical. In general, boron ionic activators may be described as salts of tetra(perfluorophenyl) boron; non-limiting examples include anilinium, carbonium, oxonium, phosphonium and sulfonium salts of tetra(perfluorophenyOboron with anilinium and trityl (or triphenylmethylium). Additional non-limiting examples of ionic activators include: triethylammonium tetra(phenyl)boron, tripropylammonium tetra(phenyl)boron, tri(n-butyl)ammonium tetra(phenyl)boron, trimethylammonium tetra(p-tolyl)boron, trimethylammonium tetra(o-tolyl)boron, tributylammonium tetra(pentafluorophenyl)boron, tripropylammonium tetra(o,p-dimethylphenyl)boron, tributylammonium tetra(m,m-dimethylphenyl)boron, tributylammonium tetra(p-trifluoromethylphenyl)boron, tributylammonium tetra(pentafluorophenyl)boron, tri(n-butyl)ammonium tetra(o-tolyl)boron, N,N-dimethylanilinium tetra(phenyl)boron, N,N-diethylanilinium tetra(phenyl)boron, N,N-diethylanilinium tetra(phenyl)n-butylboron, N,N-2,4,6-pentamethylanilinium tetra(phenyl)boron, di-(isopropyl)ammonium tetra(pentafluorophenyl)boron, dicyclohexylammonium tetra(phenyl)boron, triphenylphosphonium tetra(phenyl)boron, tri(methylphenyl)phosphonium tetra(phenyl)boron, tri(dimethylphenyl)phosphonium tetra(phenyl)boron, tropillium tetrakispentafluorophenyl borate, triphenylmethylium tetrakispentafluorophenyl borate, benzene(diazonium)tetrakispentafluorophenyl borate, tropillium tetrakis(2,3,5,6-tetrafluorophenyl)borate, triphenylmethylium tetrakis(2,3,5,6-tetrafluorophenyl)borate, benzene(diazonium)tetrakis(3,4,5-trifluorophenyl)borate, tropillium tetrakis(3,4,5-trifluorophenyl)borate, benzene(diazonium)tetrakis(3,4,5-trifluorophenyl)borate, tropillium tetrakis(1,2,2-trifluoroethenyl)borate, triphenylmethylium tetrakis(1,2,2-trifluoroethenyl)borate, benzene(diazonium)tetrakis(1,2,2-trifluoroethenyl)borate, tropillium tetrakis(2,3,4,5-tetrafluorophenyl)borate, triphenylmethylium tetrakis(2,3,4,5-tetrafluorophenyl)borate, and benzene(diazonium)tetrakis(2,3,4,5 tetrafluorophenyl)borate. Readily available commercial ionic activators include N,N-dimethylanilinium tetrakispentafluorophenyl borate, and triphenylmethylium tetrakispentafluorophenyl borate.

The optional fourth catalyst component of the single site catalyst formation is a hindered phenol, component (iv). Non-limiting example of hindered phenols include butylated phenolic antioxidants, butylated hydroxytoluene, 2,4-di-tertiarybutyl-6-ethyl phenol, 4,4′-methylenebis(2,6-di-tertiary-butylphenol), 1,3,5-trimethyl-2,4,6-tris(3,5-di-tert-butyl-4-hydroxybenzyl)benzene and octadecyl-3-(3′,5′-di-tert-butyl-4′-hydroxyphenyl) propionate.

To produce an active single site catalyst formulation the quantity and mole ratios of the three or four components, (i) through (iv) are optimized as described below.

Heterogeneous Catalyst Formulations

A number of heterogeneous catalyst formulations are well known to those skilled in the art, including, as non-limiting examples, Ziegler-Natta and chromium catalyst formulations.

In this disclosure, embodiments include an in-line and batch Ziegler-Natta catalyst formulations. The term “in-line Ziegler-Natta catalyst formulation” refers to the continuous synthesis of a small quantity of active Ziegler-Natta catalyst and immediately injecting this catalyst into at least one continuously operating reactor, where the catalyst polymerizes ethylene and one or more optional α-olefins to form an ethylene interpolymer. The terms “batch Ziegler-Natta catalyst formulation” or “batch Ziegler-Natta procatalyst” refer to the synthesis of a much larger quantity of catalyst or procatalyst in one or more mixing vessels that are external to, or isolated from, the continuously operating solution polymerization process. Once prepared, the batch Ziegler-Natta catalyst formulation, or batch Ziegler-Natta procatalyst, is transferred to a catalyst storage tank. The term “procatalyst” refers to an inactive catalyst formulation (inactive with respect to ethylene polymerization); the procatalyst is converted into an active catalyst by adding an alkyl aluminum co-catalyst. As needed, the procatalyst is pumped from the storage tank to at least one continuously operating reactor, where an active catalyst is formed and polymerizes ethylene and one or more optional α-olefins to form an ethylene interpolymer. The procatalyst may be converted into an active catalyst in the reactor or external to the reactor.

A wide variety of chemical compounds can be used to synthesize an active Ziegler-Natta catalyst formulation. The following describes various chemical compounds that may be combined to produce an active Ziegler-Natta catalyst formulation. Those skilled in the art will understand that the embodiments in this disclosure are not limited to the specific chemical compound disclosed.

An active Ziegler-Natta catalyst formulation may be formed from: a magnesium compound, a chloride compound, a metal compound, an alkyl aluminum co-catalyst and an aluminum alkyl. In Table 2A of this disclosure: “(v)” refers to “component (v)” the magnesium compound; the term “(vi)” refers to the “component (vi)” the chloride compound; “(vii)” refers to “component (vii)” the metal compound; “(viii)” refers to “component (viii)” alkyl aluminum co-catalyst, and; “(ix)” refers to “component (ix)” the aluminum alkyl. As will be appreciated by those skilled in the art, Ziegler-Natta catalyst formulations may contain additional components; a non-limiting example of an additional component is an electron donor, e.g. amines or ethers.

A non-limiting example of an active in-line Ziegler-Natta catalyst formulation can be prepared as follows. In the first step, a solution of a magnesium compound (component (v)) is reacted with a solution of the chloride compound (component (vi)) to form a magnesium chloride support suspended in solution. Non-limiting examples of magnesium compounds include Mg(R¹)₂; wherein the R¹ groups may be the same or different, linear, branched or cyclic hydrocarbyl radicals containing 1 to 10 carbon atoms. Non-limiting examples of chloride compounds include R²Cl; wherein R² represents a hydrogen atom, or a linear, branched or cyclic hydrocarbyl radical containing 1 to 10 carbon atoms. In the first step, the solution of magnesium compound may also contain an aluminum alkyl (component (ix)). Non-limiting examples of aluminum alkyl include Al(R³)₃, wherein the R³ groups may be the same or different, linear, branched or cyclic hydrocarbyl radicals containing from 1 to 10 carbon atoms. In the second step a solution of the metal compound (component (vii)) is added to the solution of magnesium chloride and the metal compound is supported on the magnesium chloride. Non-limiting examples of suitable metal compounds include M(X)_(n) or MO(X)_(n); where M represents a metal selected from Group 4 through Group 8 of the Periodic Table, or mixtures of metals selected from Group 4 through Group 8; O represents oxygen, and; X represents chloride or bromide; n is an integer from 3 to 6 that satisfies the oxidation state of the metal. Additional non-limiting examples of suitable metal compounds include Group 4 to Group 8 metal alkyls, metal alkoxides (which may be prepared by reacting a metal alkyl with an alcohol) and mixed-ligand metal compounds that contain a mixture of halide, alkyl and alkoxide ligands. In the third step a solution of an alkyl aluminum co-catalyst (component (viii)) is added to the metal compound supported on the magnesium chloride. A wide variety of alkyl aluminum co-catalysts are suitable, as expressed by formula (VI):

Al(R⁴)_(p)(OR⁵)_(q)(X)_(r)  (VI)

wherein the R⁴ groups may be the same or different, hydrocarbyl groups having from 1 to 10 carbon atoms; the OR⁵ groups may be the same or different, alkoxy or aryloxy groups wherein R⁵ is a hydrocarbyl group having from 1 to 10 carbon atoms bonded to oxygen; X is chloride or bromide, and; (p+q+r)=3, with the proviso that p is greater than 0. Non-limiting examples of commonly used alkyl aluminum co-catalysts include trimethyl aluminum, triethyl aluminum, tributyl aluminum, dimethyl aluminum methoxide, diethyl aluminum ethoxide, dibutyl aluminum butoxide, dimethyl aluminum chloride or bromide, diethyl aluminum chloride or bromide, dibutyl aluminum chloride or bromide and ethyl aluminum dichloride or dibromide.

The process described in the paragraph above, to synthesize an active in-line Ziegler-Natta catalyst formulation, can be carried out in a variety of solvents; non-limiting examples of solvents include linear or branched C₅ to C₁₂ alkanes or mixtures thereof. To produce an active in-line Ziegler-Natta catalyst formulation the quantity and mole ratios of the five components, (v) through (ix), are optimized as described below.

Additional embodiments of heterogeneous catalyst formulations include formulations where the “metal compound” is a chromium compound; non-limiting examples include silyl chromate, chromium oxide and chromocene. In some embodiments, the chromium compound is supported on a metal oxide such as silica or alumina. Heterogeneous catalyst formulations containing chromium may also include co-catalysts; non-limiting examples of co-catalysts include trialkylaluminum, alkylaluminoxane and dialkoxyalkylaluminum compounds and the like.

Solution Polymerization Process: In-Line Heterogeneous Catalyst Formulation

The ethylene interpolymer products disclosed herein, useful in the manufacture of flexible and rigid articles, were produced in a continuous solution polymerization process. This solution process has been fully described in Canadian Patent Application No. CA 2,868,640, filed Oct. 21, 2014 and entitled “SOLUTION POLYMERIZATION PROCESS”; which is incorporated by reference into this application in its entirety.

Embodiments of this process includes at least two continuously stirred reactors, R1 and R2 and an optional tubular reactor R3. Feeds (solvent, ethylene, at least two catalyst formulations, optional hydrogen and optional α-olefin) are feed to at least two reactor continuously. A single site catalyst formulation is injected into R1 and a first heterogeneous catalyst formation is injected into R2 and optionally R3. Optionally, a second heterogeneous catalyst formulation is injected into R3. The single site catalyst formulation includes an ionic activator (component (iii)), a bulky ligand-metal complex (component (i)), an alumoxane co-catalyst (component (ii)) and an optional hindered phenol (component (iv)), respectively.

R1 and R2 may be operated in series or parallel modes of operation. To be more clear, in series mode 100% of the effluent from R1 flows directly into R2. In parallel mode, R1 and R2 operate independently and the effluents from R1 and R2 are combined downstream of the reactors.

A heterogeneous catalyst formulation is injected into R2. In one embodiment a first in-line Ziegler-Natta catalyst formulation is injected into R2. A first in-line Ziegler-Natta catalyst formation is formed within a first heterogeneous catalyst assembly by optimizing the following molar ratios: (aluminum alkyl)/(magnesium compound) or (ix)/(v); (chloride compound)/(magnesium compound) or (vi)/(v); (alkyl aluminum co-catalyst)/(metal compound) or (viii)/(vii), and; (aluminum alkyl)/(metal compound) or (ix)/(vii); as well as the time these compounds have to react and equilibrate. Within the first heterogeneous catalyst assembly the time between the addition of the chloride compound and the addition of the metal compound (component (vii)) is controlled; hereafter HUT-1 (the first Hold-Up-Time). The time between the addition of component (vii) and the addition of the alkyl aluminum co-catalyst, component (viii), is also controlled; hereafter HUT-2 (the second Hold-Up-Time). In addition, the time between the addition of the alkyl aluminum co-catalyst and the injection of the in-line Ziegler-Natta catalyst formulation into R2 is controlled; hereafter HUT-3 (the third Hold-Up-Time). Optionally, 100% the alkyl aluminum co-catalyst, may be injected directly into R2. Optionally, a portion of the alkyl aluminum co-catalyst may be injected into the first heterogeneous catalyst assembly and the remaining portion injected directly into R2. The quantity of in-line heterogeneous catalyst formulation added to R2 is expressed as the parts-per-million (ppm) of metal compound (component (vii)) in the reactor solution, hereafter “R2 (vii) (ppm)”. Injection of the in-line heterogeneous catalyst formulation into R2 produces a second ethylene interpolymer in a second exit stream (exiting R2). Optionally the second exit stream is deactivated by adding a catalyst deactivator. If the second exit stream is not deactivated the second exit stream enters reactor R3. One embodiment of a suitable R3 design is a tubular reactor. Optionally, one or more of the following fresh feeds may be injected into R3; solvent, ethylene, hydrogen, α-olefin and a first or second heterogeneous catalyst formulation; the latter is supplied from a second heterogeneous catalyst assembly. The chemical composition of the first and second heterogeneous catalyst formulations may be the same, or different, i.e. the catalyst components ((v) through (ix)), mole ratios and hold-up-times may differ in the first and second heterogeneous catalyst assemblies. The second heterogeneous catalyst assembly generates an efficient catalyst by optimizing hold-up-times and the molar ratios of the catalyst components.

In reactor R3, a third ethylene interpolymer may, or may not, form. A third ethylene interpolymer will not form if a catalyst deactivator is added upstream of reactor R3. A third ethylene interpolymer will be formed if a catalyst deactivator is added downstream of R3. The optional third ethylene interpolymer may be formed using a variety of operational modes (with the proviso that catalyst deactivator is not added upstream). Non-limiting examples of operational modes include: (a) residual ethylene, residual optional α-olefin and residual active catalyst entering R3 react to form the third ethylene interpolymer, or; (b) fresh process solvent, fresh ethylene and optionally fresh α-olefin are added to R3 and the residual active catalyst entering R3 forms the third ethylene interpolymer, or; (c) a second in-line heterogeneous catalyst formulation is added to R3 to polymerize residual ethylene and residual optional α-olefin to form the third ethylene interpolymer, or; (d) fresh process solvent, ethylene, optional α-olefin and a second in-line heterogeneous catalyst formulation are added to R3 to form the third ethylene interpolymer.

In series mode, R3 produces a third exit stream (the stream exiting R3) containing the first ethylene interpolymer, the second ethylene interpolymer and optionally a third ethylene interpolymer. A catalyst deactivator may be added to the third exit stream producing a deactivated solution; with the proviso a catalyst deactivator is not added if a catalyst deactivator was added upstream of R3.

The deactivated solution passes through a pressure let down device, a heat exchanger and a passivator is added forming a passivated solution. The passivated solution passes through a series of vapor liquid separators and ultimately the ethylene interpolymer product enters polymer recover. Non-limiting examples of polymer recovery operations include one or more gear pump, single screw extruder or twin screw extruder that forces the molten ethylene interpolymer product through a pelletizer.

Embodiments of the manufactured articles disclosed herein, may also be formed from ethylene interpolymer products synthesized using a batch Ziegler-Natta catalyst. Typically, a first batch Ziegler-Natta procatalyst is injected into R2 and the procatalyst is activated within R2 by injecting an alkyl aluminum co-catalyst forming a first batch Ziegler-Natta catalyst. Optionally, a second batch Ziegler-Natta procatalyst is injected into R3.

Additional Solution Polymerization Process Parameters

A variety of solvents may be used as the process solvent; non-limiting examples include linear, branched or cyclic C₅ to C₁₂ alkanes. Non-limiting examples of α-olefins include C₃ to C₁₀ α-olefins. It is well known to individuals of ordinary experience in the art that reactor feed streams (solvent, monomer, α-olefin, hydrogen, catalyst formulation etc.) must be essentially free of catalyst deactivating poisons; non-limiting examples of poisons include trace amounts of oxygenates such as water, fatty acids, alcohols, ketones and aldehydes. Such poisons are removed from reactor feed streams using standard purification practices; non-limiting examples include molecular sieve beds, alumina beds and oxygen removal catalysts for the purification of solvents, ethylene and α-olefins, etc.

In operating the continuous solution polymerization process total amount of ethylene supplied to the process can be portioned or split between the three reactors R1, R2 and R3. This operational variable is referred to as the Ethylene Split (ES), i.e. “ES^(R1)”, “ES^(R2)” and “ES^(R3)” refer to the weight percent of ethylene injected in R1, R2 and R3, respectively; with the proviso that ES^(R1)+ES^(R2)+ES^(R3)=100%. The ethylene concentration in each reactor is also controlled. The R1 ethylene concentration is defined as the weight of ethylene in reactor 1 divided by the total weight of everything added to reactor 1; the R2 ethylene concentration (wt %) and R3 ethylene concentration (wt %) are defined similarly. The total amount of ethylene converted in each reactor is monitored. The term “Q^(R1)” refers to the percent of the ethylene added to R1 that is converted into an ethylene interpolymer by the catalyst formulation. Similarly Q^(R2) and Q^(R3) represent the percent of the ethylene added to R2 and R3 that was converted into ethylene interpolymer, in the respective reactor. The term “Q^(T)” represents the total or overall ethylene conversion across the entire continuous solution polymerization plant; i.e. Q^(T)=100×[weight of ethylene in the interpolymer product]/([weight of ethylene in the interpolymer product]+[weight of unreacted ethylene]). Optionally, α-olefin may be added to the continuous solution polymerization process. If added, α-olefin may be proportioned or split between R1, R2 and R3. This operational variable is referred to as the Comonomer Split (CS), i.e. “CS^(R1)”, “CS^(R2)” and “CS^(R3)” refer to the weight percent of α-olefin comonomer that is injected in R1, R2 and R3, respectively; with the proviso that CS^(R1)+CS^(R2)+CS^(R3)=100%.

In the continuous polymerization processes described, polymerization is terminated by adding a catalyst deactivator. The catalyst deactivator substantially stops the polymerization reaction by changing active catalyst species to inactive forms. Suitable deactivators are well known in the art, non-limiting examples include: amines (e.g. U.S. Pat. No. 4,803,259 to Zboril et al.); alkali or alkaline earth metal salts of carboxylic acid (e.g. U.S. Pat. No. 4,105,609 to Machan et al.); water (e.g. U.S. Pat. No. 4,731,438 to Bernier et al.); hydrotalcites, alcohols and carboxylic acids (e.g. U.S. Pat. No. 4,379,882 to Miyata); or a combination thereof (U.S. Pat. No. 6,180,730 to Sibtain et al.).

Prior to entering the vapor/liquid separator, a passivator or acid scavenger is added to deactivated solution. Suitable passivators are well known in the art, non-limiting examples include alkali or alkaline earth metal salts of carboxylic acids or hydrotalcites.

In this disclosure, the number of solution reactors is not particularly important; with the proviso that the continuous solution polymerization process comprises at least two reactors that employ at least one single-site catalyst formulation and at least one heterogeneous catalyst formulation.

First Ethylene Interpolymer

The first ethylene interpolymer is produced with a single-site catalyst formulation. If the optional α-olefin is not added to reactor 1 (R1), then the ethylene interpolymer produced in R1 is an ethylene homopolymer. If an α-olefin is added, the following weight ratio is one parameter to control the density of the first ethylene interpolymer: ((α-olefin)/(ethylene))^(R1). The symbol “σ¹” refers to the density of the first ethylene interpolymer produced in R1. The upper limit on σ¹ may be about 0.975 g/cm³; in some cases about 0.965 g/cm³ and; in other cases about 0.955 g/cm³. The lower limit on σ¹ may be about 0.855 g/cm³, in some cases about 0.865 g/cm³, and; in other cases about 0.875 g/cm³.

Methods to determine the CDBI₅₀ (Composition Distribution Branching Index) of an ethylene interpolymer are well known to those skilled in the art. The CDBI₅₀, expressed as a percent, is defined as the percent of the ethylene interpolymer whose comonomer composition is within 50% of the median comonomer composition. It is also well known to those skilled in the art that the CDBI₅₀ of ethylene interpolymers produced with single-site catalyst formulations are higher relative to the CDBI₅₀ of α-olefin containing ethylene interpolymers produced with heterogeneous catalyst formulations. The upper limit on the CDBI₅₀ of the first ethylene interpolymer (produced with a single-site catalyst formulation) may be about 98%, in other cases about 95% and in still other cases about 90%. The lower limit on the CDBI₅₀ of the first ethylene interpolymer may be about 70%, in other cases about 75% and in still other cases about 80%.

As is well known to those skilled in the art the M_(w)/M_(n) of ethylene interpolymers produced with single site catalyst formulations are lower relative to ethylene interpolymers produced with heterogeneous catalyst formulations. Thus, in the embodiments disclosed, the first ethylene interpolymer has a lower M_(w)/M_(n) relative to the second ethylene interpolymer; where the second ethylene interpolymer is produced with a heterogeneous catalyst formulation. The upper limit on the M_(w)/M_(n) of the first ethylene interpolymer may be about 2.8, in other cases about 2.5 and in still other cases about 2.2. The lower limit on the M_(w)/M_(n) the first ethylene interpolymer may be about 1.7, in other cases about 1.8 and in still other cases about 1.9.

The first ethylene interpolymer contains catalyst residues that reflect the chemical composition of the single-site catalyst formulation used. Those skilled in the art will understand that catalyst residues are typically quantified by the parts per million of metal in the first ethylene interpolymer, where metal refers to the metal in component (i), i.e. the metal in the “bulky ligand-metal complex”; hereafter (and in the claims) this metal will be referred to “metal A”. As recited earlier in this disclosure, non-limiting examples of metal A include Group 4 metals, titanium, zirconium and hafnium. The upper limit on the ppm of metal A in the first ethylene interpolymer may be about 1.0 ppm, in other cases about 0.9 ppm and in still other cases about 0.8 ppm. The lower limit on the ppm of metal A in the first ethylene interpolymer may be about 0.01 ppm, in other cases about 0.1 ppm and in still other cases about 0.2 ppm.

The amount of hydrogen added to R1 can vary over a wide range allowing the continuous solution process to produce first ethylene interpolymers that differ greatly in melt index, hereafter I₂ ¹ (melt index is measured at 190° C. using a 2.16 kg load following the procedures outlined in ASTM D1238). The quantity of hydrogen added to R1 is expressed as the parts-per-million (ppm) of hydrogen in R1 relative to the total mass in reactor R1; hereafter H₂ ^(R1) (ppm). The upper limit on I₂ ¹ may be about 200 dg/min, in some cases about 100 dg/min; in other cases about 50 dg/min, and; in still other cases about 1 dg/min. The lower limit on I₂ ¹ may be about 0.01 dg/min, in some cases about 0.05 dg/min; in other cases about 0.1 dg/min, and; in still other cases about 0.5 dg/min.

The upper limit on the weight percent (wt %) of the first ethylene interpolymer in the ethylene interpolymer product may be about 60 wt %, in other cases about 55 wt % and in still other cases about 50 wt %. The lower limit on the wt % of the first ethylene interpolymer in the ethylene interpolymer product may be about 15 wt %; in other cases about 25 wt % and in still other cases about 30 wt %.

Second Ethylene Interpolymer

If optional α-olefin is not added to reactor 2 (R2) either by adding fresh α-olefin to R2 (or carried over from R1) then the ethylene interpolymer produced in R2 is an ethylene homopolymer. If an optional α-olefin is present in R2, the following weight ratio is one parameter to control the density of the second ethylene interpolymer produced in R2: ((α-olefin)/(ethylene))^(R2). Hereafter, the symbol “σ²” refers to the density of the ethylene interpolymer produced in R2. The upper limit on σ² may be about 0.975 g/cm³; in some cases about 0.965 g/cm³ and; in other cases about 0.955 g/cm³. Depending on the heterogeneous catalyst formulation used, the lower limit on σ² may be about 0.89 g/cm³, in some cases about 0.90 g/cm³, and; in other cases about 0.91 g/cm³.

A heterogeneous catalyst formulation is used to produce the second ethylene interpolymer. If the second ethylene interpolymer contains an α-olefin, the CDBI₅₀ of the second ethylene interpolymer is lower relative to the CDBI₅₀ of the first ethylene interpolymer that was produced with a single-site catalyst formulation. In an embodiment of this disclosure, the upper limit on the CDBI₅₀ of the second ethylene interpolymer (that contains an α-olefin) may be about 70%, in other cases about 65% and in still other cases about 60%. In an embodiment of this disclosure, the lower limit on the CDBI₅₀ of the second ethylene interpolymer (that contains an α-olefin) may be about 45%, in other cases about 50% and in still other cases about 55%. If an α-olefin is not added to the continuous solution polymerization process the second ethylene interpolymer is an ethylene homopolymer. In the case of a homopolymer, which does not contain α-olefin, one can still measure a CDBI₅₀ using TREF. In the case of a homopolymer, the upper limit on the CDBI₅₀ of the second ethylene interpolymer may be about 98%, in other cases about 96% and in still other cases about 95%, and; the lower limit on the CDBI₅₀ may be about 88%, in other cases about 89% and in still other cases about 90%. It is well known to those skilled in the art that as the α-olefin content in the second ethylene interpolymer approaches zero, there is a smooth transition between the recited CDBI₅₀ limits for the second ethylene interpolymers (that contain an α-olefin) and the recited CDBI₅₀ limits for the second ethylene interpolymers that are ethylene homopolymers. Typically, the CDBI₅₀ of the first ethylene interpolymer is higher than the CDBI₅₀ of the second ethylene interpolymer.

The M_(w)/M_(n) of second ethylene interpolymer is higher than the M_(w)/M_(n) of the first ethylene interpolymer. The upper limit on the M_(w)/M_(n) of the second ethylene interpolymer may be about 4.4, in other cases about 4.2 and in still other cases about 4.0. The lower limit on the M_(w)/M_(n) of the second ethylene interpolymer may be about 2.2. M_(w)/M_(n)'s of 2.2 are observed when the melt index of the second ethylene interpolymer is high, or when the melt index of the ethylene interpolymer product is high, e.g. greater than 10 g/10 minutes. In other cases the lower limit on the M_(w)/M_(n) of the second ethylene interpolymer may be about 2.4 and in still other cases about 2.6.

The second ethylene interpolymer contains catalyst residues that reflect the chemical composition of heterogeneous catalyst formulation. Those skilled in the art with understand that heterogeneous catalyst residues are typically quantified by the parts per million of metal in the second ethylene interpolymer, where the metal refers to the metal originating from component (vii), i.e. the “metal compound”; hereafter (and in the claims) this metal will be referred to as “metal B”. As recited earlier in this disclosure, non-limiting examples of metal B include metals selected from Group 4 through Group 8 of the Periodic Table, or mixtures of metals selected from Group 4 through Group 8. The upper limit on the ppm of metal B in the second ethylene interpolymer may be about 12 ppm, in other cases about 10 ppm and in still other cases about 8 ppm. The lower limit on the ppm of metal B in the second ethylene interpolymer may be about 0.5 ppm, in other cases about 1 ppm and in still other cases about 3 ppm. While not wishing to be bound by any particular theory, in series mode of operation it is believed that the chemical environment within the second reactor deactivates the single site catalyst formulation, or; in parallel mode of operation the chemical environment within R2 deactivates the single site catalyst formation.

The amount of hydrogen added to R2 can vary over a wide range which allows the continuous solution process to produce second ethylene interpolymers that differ greatly in melt index, hereafter I₂ ². The quantity of hydrogen added is expressed as the parts-per-million (ppm) of hydrogen in R2 relative to the total mass in reactor R2; hereafter H₂ ^(R2) (ppm). The upper limit on I₂ ² may be about 1000 dg/min; in some cases about 750 dg/min; in other cases about 500 dg/min, and; in still other cases about 200 dg/min. The lower limit on I₂ ² may be about 0.3 dg/min, in some cases about 0.4 dg/min, in other cases about 0.5 dg/min, and; in still other cases about 0.6 dg/min.

The upper limit on the weight percent (wt %) of the second ethylene interpolymer in the ethylene interpolymer product may be about 85 wt %, in other cases about 80 wt % and in still other cases about 70 wt %. The lower limit on the wt % of the second ethylene interpolymer in the ethylene interpolymer product may be about 30 wt %; in other cases about 40 wt % and in still other cases about 50 wt %.

Third Ethylene Interpolymer

A third ethylene interpolymer is not produced in R3 if a catalyst deactivator is added upstream of R3. If a catalyst deactivator is not added and optional α-olefin is not present then the third ethylene interpolymer produced in R3 is an ethylene homopolymer. If a catalyst deactivator is not added and optional α-olefin is present in R3, the following weight ratio determines the density of the third ethylene interpolymer: ((α-olefin)/(ethylene))R³. In the continuous solution polymerization process ((α-olefin)/(ethylene))R³ is one of the control parameter used to produce a third ethylene interpolymer with a desired density. Hereafter, the symbol “σ³” refers to the density of the ethylene interpolymer produced in R3. The upper limit on σ³ may be about 0.975 g/cm³; in some cases about 0.965 g/cm³ and; in other cases about 0.955 g/cm³. Depending on the heterogeneous catalyst formulations used, the lower limit on σ³ may be about 0.89 g/cm³, in some cases about 0.90 g/cm³, and; in other cases about 0.91 g/cm³. Optionally, a second heterogeneous catalyst formulation may be added to R3.

Typically, the upper limit on the CDBI₅₀ of the optional third ethylene interpolymer (containing an α-olefin) may be about 65%, in other cases about 60% and in still other cases about 55%. The CDBI₅₀ of an α-olefin containing optional third ethylene interpolymer will be lower than the CDBI₅₀ of the first ethylene interpolymer produced with the single-site catalyst formulation. Typically, the lower limit on the CDBI₅₀ of the optional third ethylene interpolymer (containing an α-olefin) may be about 35%, in other cases about 40% and in still other cases about 45%. If an α-olefin is not added to the continuous solution polymerization process the optional third ethylene interpolymer is an ethylene homopolymer. In the case of an ethylene homopolymer the upper limit on the CDBI₅₀ may be about 98%, in other cases about 96% and in still other cases about 95%, and; the lower limit on the CDBI₅₀ may be about 88%, in other cases about 89% and in still other cases about 90%. Typically, the CDBI₅₀ of the first ethylene interpolymer is higher than the CDBI₅₀ of the third ethylene interpolymer and second ethylene interpolymer.

The upper limit on the M_(w)/M_(n) of the optional third ethylene interpolymer may be about 5.0, in other cases about 4.8 and in still other cases about 4.5. The lower limit on the M_(w)/M_(n) of the optional third ethylene interpolymer may be about 2.2, in other cases about 2.4 and in still other cases about 2.6. The M_(w)/M_(n) of the optional third ethylene interpolymer is higher than the M_(w)/M_(n) of the first ethylene interpolymer. When blended together, the second and third ethylene interpolymer have a fourth M_(w)/M_(n) which is not broader than the M_(w)/M_(n) of the second ethylene interpolymer.

The catalyst residues in the optional third ethylene interpolymer reflect the chemical composition of the heterogeneous catalyst formulation(s) used, i.e. the first and optionally a second heterogeneous catalyst formulation. The chemical compositions of the first and second heterogeneous catalyst formulations may be the same or different; for example a first component (vii) and a second component (vii) may be used to synthesize the first and second heterogeneous catalyst formulation. As recited above, “metal B” refers to the metal that originates from the first component (vii). Hereafter, “metal C” refers to the metal that originates from the second component (vii). Metal B and optional metal C may be the same, or different. Non-limiting examples of metal B and metal C include metals selected from Group 4 through Group 8 of the Periodic Table, or mixtures of metals selected from Group 4 through Group 8. The upper limit on the ppm of (metal B+metal C) in the optional third ethylene interpolymer may be about 12 ppm, in other cases about 10 ppm and in still other cases about 8 ppm. The lower limit on the ppm of (metal B+metal C) in the optional third ethylene interpolymer may be about 0.5 ppm, in other cases about 1 ppm and in still other cases about 3 ppm.

Optionally hydrogen may be added to R3. Adjusting the amount of hydrogen in R3, hereafter H₂ ^(R3) (ppm), allows the continuous solution process to produce third ethylene interpolymers that differ widely in melt index, hereafter I₂ ³. The upper limit on I₂ ³ may be about 2000 dg/min; in some cases about 1500 dg/min; in other cases about 1000 dg/min, and; in still other cases about 500 dg/min. The lower limit on I₂ ³ may be about 0.5 dg/min, in some cases about 0.6 dg/min, in other cases about 0.7 dg/min, and; in still other cases about 0.8 dg/min.

The upper limit on the weight percent (wt %) of the optional third ethylene interpolymer in the ethylene interpolymer product may be about 30 wt %, in other cases about 25 wt % and in still other cases about 20 wt %. The lower limit on the wt % of the optional third ethylene interpolymer in the ethylene interpolymer product may be 0 wt %; in other cases about 5 wt % and in still other cases about 10 wt %.

Ethylene Interpolymer Product

The upper limit on the density of the ethylene interpolymer product may be about 0.975 g/cm³; in some cases about 0.965 g/cm³ and; in other cases about 0.955 g/cm³. The lower limit on the density of the ethylene interpolymer product may be about 0.869 g/cm³, in some cases about 0.879 g/cm³, and; in other cases about 0.889 g/cm³.

The upper limit on the CDBI₅₀ of the ethylene interpolymer product may be about 97%, in other cases about 90% and in still other cases about 85%. An ethylene interpolymer product with a CDBI₅₀ of 97% may result if an α-olefin is not added to the continuous solution polymerization process; in this case, the ethylene interpolymer product is an ethylene homopolymer. The lower limit on the CDBI₅₀ of an ethylene interpolymer may be about 20%, in other cases about 40% and in still other cases about 60%.

The upper limit on the M_(w)/M_(n) of the ethylene interpolymer product may be about 25, in other cases about 15 and in still other cases about 9. The lower limit on the M_(w)/M_(n) of the ethylene interpolymer product may be 2.0, in other cases about 2.2 and in still other cases about 2.4.

The catalyst residues in the ethylene interpolymer product reflect the chemical compositions of: the single-site catalyst formulation employed in R1; the first heterogeneous catalyst formulation employed in R2, and; optionally the first or optionally the first and second heterogeneous catalyst formulation employed in R3. In this disclosure, catalyst residues were quantified by measuring the parts per million of catalytic metal in the ethylene interpolymer products. In addition, the elemental quantities (ppm) of magnesium, chlorine and aluminum were quantified. Catalytic metals originate from two or optionally three sources, specifically: 1) “metal A” that originates from component (i) that was used to form the single-site catalyst formulation; (2) “metal B” that originates from the first component (vii) that was used to form the first heterogeneous catalyst formulation, and; (3) optionally “metal C” that originates from the second component (vii) that was used to form the optional second heterogeneous catalyst formulation. Metals A, B and C may be the same or different. In this disclosure the term “total catalytic metal” is equivalent to the sum of catalytic metals A+B+C. Further, in this disclosure the terms “first total catalytic metal” and “second total catalyst metal” are used to differentiate between the first ethylene interpolymer product of this disclosure and a comparative “polyethylene composition” that were produced using different catalyst formulations.

The upper limit on the ppm of metal A in the ethylene interpolymer product may be about 0.6 ppm, in other cases about 0.5 ppm and in still other cases about 0.4 ppm. The lower limit on the ppm of metal A in the ethylene interpolymer product may be about 0.001 ppm, in other cases about 0.01 ppm and in still other cases about 0.03 ppm. The upper limit on the ppm of (metal B+metal C) in the ethylene interpolymer product may be about 11 ppm, in other cases about 9 ppm and in still other cases about 7 ppm. The lower limit on the ppm of (metal B+metal C) in the ethylene interpolymer product may be about 0.5 ppm, in other cases about 1 ppm and in still other cases about 3 ppm.

In some embodiments, ethylene interpolymers may be produced where the catalytic metals (metal A, metal B and metal C) are the same metal; a non-limiting example would be titanium. In such embodiments, the ppm of (metal B+metal C) in the ethylene interpolymer product is calculated using equation (VII):

ppm^((B+C))=(ppm^((A+B+C))−(f ^(A)×ppm^(A)))/(1−f ^(A))  (VII)

where: ppm^((B+C)) is the calculated ppm of (metal B+metal C) in the ethylene interpolymer product; ppm^((A+B+C)) is the total ppm of catalyst residue in the ethylene interpolymer product as measured experimentally, i.e. (metal A ppm+metal B ppm+metal C ppm); f^(A) represents the weight fraction of the first ethylene interpolymer in the ethylene interpolymer product, f^(A) may vary from about 0.15 to about 0.6, and; ppm^(A) represents the ppm of metal A in the first ethylene interpolymer. In equation (VII) ppm^(A) is assumed to be 0.35 ppm.

Embodiments of the ethylene interpolymer products disclosed herein have lower catalyst residues relative to the polyethylene polymers described in U.S. Pat. No. 6,277,931. Higher catalyst residues in U.S. Pat. No. 6,277,931 increase the complexity of the continuous solution polymerization process; an example of increased complexity includes additional purification steps to remove catalyst residues from the polymer. In contrast, in the present disclosure, catalyst residues are not removed. In this disclosure, the upper limit on the “total catalytic metal”, i.e. the total ppm of (metal A ppm+metal B ppm+optional metal C ppm) in the ethylene interpolymer product may be about 11 ppm, in other cases about 9 ppm and in still other cases about 7, and; the lower limit on the total ppm of catalyst residuals (metal A+metal B+optional metal C) in the ethylene interpolymer product may be about 0.5 ppm, in other cases about 1 ppm and in still other cases about 3 ppm.

The upper limit on melt index of the ethylene interpolymer product may be about 500 dg/min, in some cases about 400 dg/min; in other cases about 300 dg/min, and; in still other cases about 200 dg/min. The lower limit on the melt index of the ethylene interpolymer product may be about 0.3 dg/min, in some cases about 0.4 dg/min; in other cases about 0.5 dg/min, and; in still other cases about 0.6 dg/min.

A computer generated ethylene interpolymer product is illustrated in Table 1; this simulations was based on fundamental kinetic models (with kinetic constants specific for each catalyst formulation) as well as feed and reactor conditions. The simulation was based on the configuration of the solution pilot plant described below; which was used to produce the examples of ethylene interpolymer products disclosed herein. Simulated Example 13 was synthesized using a single-site catalyst formulation (PIC-1) in R1 and an in-line Ziegler-Natta catalyst formulation in R2 and R3. Table 1 discloses a non-limiting example of the density, melt index and molecular weights of the first, second and third ethylene interpolymers produced in the three reactors (R1, R2 and R3); these three interpolymers are combined to produce Simulated Example 13 (the ethylene polymer product). As shown in Table 1, the Simulated Example 13 product has a density of 0.9169 g/cm³, a melt index of 1.0 dg/min, a branch frequency of 12.1 (the number of C₆-branches per 1000 carbon atoms (1-octene comonomer)) and a M_(w)/M_(n) of 3.11. Simulated Example 13 comprises: a first, second and third ethylene interpolymer having a first, second and third melt index of 0.31 dg/min, 1.92 dg/min and 4.7 dg/min, respectively; a first, second and third density of 0.9087 g/cm³, 0.9206 g/cm³ and 0.9154 g/cm³, respectively; a first, second and third M_(w)/M_(n) of 2.03 M_(w)/M_(n), 3.29 M_(w)/M_(n) and 3.28 M_(w)/M_(n), respectively, and; a first, second and third CDBI₅₀ of 90 to 95%, 55 to 60% and 45 to 55%, respectively. The simulated production rate of Simulated Example 13 was 90.9 kg/hr and the R3 exit temperature was 217.1° C.

Ethylene Interpolymer Products Suitable for Films, Containers and Lids

Tables 2A through 2C summarize process conditions that were used to produce Examples 20-24 as well as Comparative Example 10. The production rates of Examples 20-24 were at least 23% higher relative to Comparative Example 10. In Examples 20-24 a single-site catalyst formulation was employed in reactor 1 and an in-line Ziegler-Natta catalyst formulations was employed in reactor 2, producing an ethylene interpolymer products having production rates from 93.1 to 99.4 kg/h. In contrast, in Comparative Example 10 a single-site catalyst formulation was used in both reactors 1 and 2, producing “a comparative ethylene interpolymer” at a maximum production rate of 75.8 kg/hr. In the case of the mixed catalyst system (Examples 20-24) the production rate was at least 23% improved (higher), relative to Comparative Example 10. In Examples 20-24 and Comparative Example 10, reactors 1 and 2 were configured in series, i.e. the effluent from reactor 1 flowed directly into reactor 2.

Table 3 summarizes the density, melt flow properties and molecular weights of Examples 20-24 and Comparative Example 10. FIG. 1 shows the GPC chromatograms of Examples 20-22 and 24, as well as Comparative Example 10. Example 20 has a unimodal molecular weight distribution (M_(w)/M_(n)=3.19), Example 24 has a bimodal molecular weight distribution (M_(w)/M_(n)=5.27) and Comparative Example 10 has a distinctly bimodal molecular weight distribution (M_(w)/M_(n)=9.25). Comparative Example 10 was synthesized using a single site catalyst formulation in both reactor 1 and reactor 2.

Table 4 compares the melt strengths of Examples 20-24 with Comparative Examples G1-G8. Comparative Examples G1-G8 are eight samples of a commercial resin designated SURPASS® HPs167-AB available from NOVA Chemicals (Calgary, AB, Canada). HPs167-AB is produced in a continuous solution polymerization process employing a single-site catalyst formulation in reactor 1 and reactor 2, where the two reactors are connected in series. The average melt index (12) of Comparative Examples G1-G8 was 1.12 dg/min and the average melt strength was 2.7cN. FIG. 2 illustrates the data in Table 4 and the following regression relationship that was fit to Examples 20-24.

(AHO Melt Strength)=7.8280−5.6363×I ₂+1.5087×I ₂ ²

Based on this regression relationships, an ethylene interpolymer product of this disclosure, having a melt index (12) of 1.12 dg/min, has a melt strength of 3.3 cN. Thus the ethylene interpolymers disclosed herein have a melt strength that is 23% higher, relative to the melt strength of Comparative Examples G1-G8, i.e. 2.7cN. Based on Table 4 and FIG. 2 ethylene interpolymer products comprising a first ethylene interpolymer synthesized using a single-site catalyst formulation, a second ethylene interpolymer synthesized using a Ziegler-Natta catalyst formulation and optionally a third ethylene interpolymer synthesized using a Ziegler-Natta catalyst formulation have about 5% to 30% higher AHO melt strength; relative to comparative ethylene interpolymer comprising a fourth and fifth ethylene interpolymer synthesized using the single-site catalyst formulation.

Examples 20-24 were passed through a twin screw extruder where 1200 ppm of a nucleating agent was thoroughly blended with the ethylene interpolymer products. The nucleating agent added was a commercial product HPN-20E (available from Milliken & Company, Spartanburgh, S.C., USA); HPN-20E is a blend of a calcium and zinc salts of 1,2-cyclohexanedicarboxylkic acid. Table 5 and FIG. 3 illustrate the influence of melt flow properties (melt index (I₂) and melt flow ratio (MFR or I₂₁/I₂)) and nucleation on the density of ethylene interpolymer products.

Table 6 compares the half times of crystallization (t_(1/2)) of Examples 20-24 and Comparative Example 10. As shown in FIG. 4, the ethylene interpolymers of this disclosure, Examples 20-24, have significantly lower half times of crystallization relative to Comparative Example 10. The average half time of crystallization of Examples 20-24 was 9.91±2.38 s, relative to 51.6 s for Comparative Example 10. Thus the disclosed ethylene interpolymer products have an average half time of crystallization that is improved (reduced) 81% relative to Comparative Example 10. In other words, relative to Comparative Example 10, the disclosed ethylene interpolymer crystallize significantly faster. Ethylene interpolymer products having faster crystallization rates are useful and of great value in many applications; a non-limiting example includes injection molding applications where more rapid crystallization allows parts to “set up” or harden more quickly, thus more parts can be produced per hour. Based on Table 6 and FIG. 4 ethylene interpolymer products comprising a first ethylene interpolymer synthesized using a single-site catalyst formulation, a second ethylene interpolymer synthesized using a Ziegler-Natta catalyst formulation and optionally a third ethylene interpolymer synthesized using a Ziegler-Natta catalyst formulation have at least 70% lower half time of crystallization (t_(1/2)); relative to comparative ethylene interpolymer comprising a fourth and fifth ethylene interpolymer synthesized using the single-site catalyst formulation.

The right most column of Table 6 compares the half times of crystallization (t_(1/2)) of nucleated Examples 20-24 and nucleated Comparative Example 10; where 1200 ppm of nucleating agent was added via twin screw melt mixing. In this disclosure a nucleating agent, or clarifying agent, is meant to be any material that effectively accelerates the phase change from a molten ethylene interpolymer to a solid semi-crystalline ethylene interpolymer; non-limiting examples of techniques to quantify the efficacy of the nucleating agent include, lower half times of crystallization as measured using a differential scanning calorimeter or measuring the reduction in crystal size as measured using an optical microscope. As shown in FIG. 5, the nucleated ethylene interpolymers of this disclosure, have significantly lower half times of crystallization relative to the nucleated comparative example, i.e. the average half time of crystallization of nucleated Examples 20-24 was 1.73±0.08 s, relative to 3.09 s for nucleated Comparative Example 10. Thus the disclosed nucleated ethylene interpolymer products have an average half time of crystallization that is improved (reduced) 44% relative to nucleated Comparative Example 10. Nucleated ethylene interpolymer products having faster crystallization rates are useful and of great value in many applications; a non-limiting example include barrier film applications where lower water vapor transmission rates are desired in food packaging.

Table 7 compares the heat deflection temperatures (HDT) of Examples 20-24 and Comparative Example 10. In graphical form, FIG. 6 shows all the data tabulated in Table 7. The solid line in FIG. 6 is a linear regression relationship fit to Examples 20-24, both non-nucleated and nucleated samples, i.e.

HDT=−1268.3+1402.1×Density

where ‘Density’ is the density (g/cc) of the non-nucleated or nucleated samples. The dotted line is a visual fit to Comparative Example 10, both non-nucleated and nucleated, assuming a slope of 1402.1° C./(g/cc). FIG. 6 shows that Examples 20-24 have a 6.6° C. higher heat deflection temperature, relative to Comparative Example 10; at 0.958 g/cc an ethylene interpolymer product of this disclosure has a 9.6% higher heat deflection temperature relative to a comparative ethylene interpolymer, and; at 0.968 g/cc, an ethylene interpolymer product of this disclosure has an 8.0% higher heat deflection temperature relative to a comparative ethylene interpolymer. Based on Table 7 and FIG. 6 ethylene interpolymer products comprising a first ethylene interpolymer synthesized using a single-site catalyst formulation, a second ethylene interpolymer synthesized using a Ziegler-Natta catalyst formulation and optionally a third ethylene interpolymer synthesized using a Ziegler-Natta catalyst formulation have about 4° C. to about 10° C. higher heat deflection temperatures (HDT); relative to comparative ethylene interpolymer comprising a fourth and fifth ethylene interpolymer synthesized using the single-site catalyst formulation. Ethylene interpolymer products having higher heat deflection temperatures are useful and valued in many applications. Non-limiting examples include: injection molding applications where a molded part maintains its dimensional stability at higher temperatures, i.e. the molded part has a higher upper use temperature and is functional over a wider temperature range, and; higher heat deflection temperatures are also desirable in film applications, for example in the packaging of hot foods, or the cooking of foods within a thin film comprising a least one layer of ethylene interpolymer product having a higher heat deflection temperature.

The un-nucleated ethylene interpolymers of this disclosure were converted in 1.5 mil (38 μm) film using an OCS cast film line and the physical properties of these films are summarized in Table 8. Similarly, the nucleated ethylene interpolymers of this disclosure were converted in 1.5 mil film and the physical properties of these films are summarized in Table 9.

Dilution Index (Y_(d)) of Ethylene Interpolymer Products

In FIG. 7 the Dilution Index (Y_(d), having dimensions of ° (degrees)) and Dimensionless Modulus (X_(d)) are plotted for several embodiments of the ethylene interpolymer products disclosed herein (the solid symbols), as well as comparative ethylene interpolymer products, i.e. Comparative A, D, E and S. Further, FIG. 7 defines the following three quadrants:

Type I: Y_(d)>0 and X_(d)<0;

Type II: Y_(d)>0 and X_(d)>0, and;

Type III: Y_(d)<0 and X_(d)>0.

The data plotted in FIG. 7 is also tabulated in Table 10. In FIG. 7, Comparative S (open triangle) was used as the rheological reference in the Dilution Index test protocol. Comparative S is an ethylene interpolymer product comprising an ethylene interpolymer synthesized using an in-line Ziegler-Natta catalyst in one solution reactor, i.e. SCLAIR® FP120-C which is an ethylene/1-octene interpolymer available from NOVA Chemicals Company (Calgary, Alberta, Canada). Comparatives D and E (open diamonds, Y_(d)<0, X_(d)>0) are ethylene interpolymer products comprising a first ethylene interpolymer synthesized using a single-site catalyst formation and a second ethylene interpolymer synthesized using a batch Ziegler-Natta catalyst formulation employing a dual reactor solution process, i.e. Elite® 5100G and Elite® 5400G, respectively, both ethylene/1-octene interpolymers available from The Dow Chemical Company (Midland, Mich., USA). Comparative A (open square, Y_(d)>0 and X_(d)<0) was an ethylene interpolymer product comprising a first and second ethylene interpolymer synthesized using a single-site catalyst formation in a dual reactor solution process, i.e. SURPASS® FPs117-C which is an ethylene/1-octene interpolymer available from NOVA Chemicals Company (Calgary, Alberta, Canada).

The following defines the Dilution Index (Y_(d)) and Dimensionless Modulus (X_(d)). In addition to having molecular weights, molecular weight distributions and branching structures, blends of ethylene interpolymers may exhibit a hierarchical structure in the melt phase. In other words, the ethylene interpolymer components may be, or may not be, homogeneous down to the molecular level depending on interpolymer miscibility and the physical history of the blend. Such hierarchical physical structure in the melt is expected to have a strong impact on flow and hence on processing and converting; as well as the end-use properties of manufactured articles. The nature of this hierarchical physical structure between interpolymers can be characterized.

The hierarchical physical structure of ethylene interpolymers can be characterized using melt rheology. A convenient method can be based on the small amplitude frequency sweep tests. Such rheology results are expressed as the phase angle gas a function of complex modulus G*, referred to as van Gurp-Palmen plots (as described in M. Van Gurp, J. Palmen, Rheol. Bull. (1998) 67(1): 5-8, and; Dealy J, Plazek D. Rheol. Bull. (2009) 78(2): 16-31). For a typical ethylene interpolymer, the phase angle δ increases toward its upper bound of 90° with G* becoming sufficiently low. A typical VGP plot is shown in FIG. 8. The VGP plots are a signature of resin architecture. The rise of δ toward 90° is monotonic for an ideally linear, monodisperse interpolymer. The δ(G*) for a branched interpolymer or a blend containing a branched interpolymer may show an inflection point that reflects the topology of the branched interpolymer (see S. Trinkle, P. Walter, C. Friedrich, Rheo. Acta (2002) 41: 103-113). The deviation of the phase angle δ from the monotonic rise may indicate a deviation from the ideal linear interpolymer either due to presence of long chain branching if the inflection point is low (e.g., δ≦20°) or a blend containing at least two interpolymers having dissimilar branching structure if the inflection point is high (e.g., δ≧70°).

For commercially available linear low density polyethylenes, inflection points are not observed; with the exception of some commercial polyethylenes that contain a small amount of long chain branching (LCB). To use the VGP plots regardless of presence of LCB, an alternative is to use the point where the frequency ω_(c) is two decades below the cross-over frequency ω_(c), i.e., ω_(c)=0.01ω_(x). The cross-over point is taken as the reference as it is known to be a characteristic point that correlates with MI, density and other specifications of an ethylene interpolymer. The cross-over modulus is related to the plateau modulus for a given molecular weight distribution (see S. Wu. J Polym Sci, Polym Phys Ed (1989) 27:723; M. R. Nobile, F. Cocchini. Rheol Acta (2001) 40:111). The two decade shift in phase angle δ is to find the comparable points where the individual viscoelastic responses of constituents could be detected; to be more clear, this two decade shift is shown in FIG. 9. The complex modulus G*_(c) for this point is normalized to the cross-over modulus, G*_(x)/(√{square root over (2)}), as (√{square root over (2)})G*_(c)/G*_(x), to minimize the variation due to overall molecular weight, molecular weight distribution and the short chain branching. As a result, the coordinates on VGP plots for this low frequency point at ω_(c)=0.01ω_(x), namely (√{square root over (2)})G*_(c)/G*_(x) and δ_(c), characterize the contribution due to blending. Similar to the inflection points, the closer the ((√{square root over (2)})G*_(c)/G*_(x), δ_(c)) point is toward the 90° upper bound, the more the blend behaves as if it were an ideal single component.

As an alternative way to avoid interference due to the molecular weight, molecular weight distribution and the short branching of the ethylene δ_(c) interpolymer ingredients, the coordinates (G*_(c),δ_(c)) are compared to a reference sample of interest to form the following two parameters:

“Dilution Index (Y_(d))”

Y _(d)=δ_(c)−(C ₀ −C ₁ e ^(C) ² ^(inG*) ^(c) )

“Dimensionless Modulus (X_(d))”

X _(d) =G* _(0.01ω) _(c) /G* _(r)

The constants C₀, C₁, and C₂ are determined by fitting the VGP data δ(G*) of the reference sample to the following equation:

δ=C ₀ −C ₁ e ^(C) ² ^(lnG*)

G*_(r) is the complex modulus of this reference sample at its δ_(c)=(0.01ω_(x)). When an ethylene interpolymer, synthesized with an in-line Ziegler-Natta catalyst employing one solution reactor, having a density of 0.920 g/cm³ and a melt index (MI or I₂) of 1.0 dg/min is taken as a reference sample, the constants are:

C₀=93.43°

C₁=1.316°

C₂=0.2945

G*_(r)=9432 Pa.

The values of these constants can be different if the rheology test protocol differs from that specified herein.

These regrouped coordinates (X_(d), Y_(d)) from (G*_(c), δ_(c)) allows comparison between ethylene interpolymer products disclosed herein with Comparative examples. The Dilution Index (Y_(d)) reflects whether the blend behaves like a simple blend of linear ethylene interpolymers (lacking hierarchical structure in the melt) or shows a distinctive response that reflects a hierarchical physical structure within the melt. The lower the Y_(d), the more the sample shows separate responses from the ethylene interpolymers that comprise the blend; the higher the Y_(d) the more the sample behaves like a single component, or single ethylene interpolymer.

Returning to FIG. 7: Type I (upper left quadrant)ethylene interpolymer products of this disclosure (solid symbols) have Y_(d)>0; in contrast, Type III (lower right quadrant) comparative ethylene interpolymers, Comparative D and E have Y_(d)<0. In the case of Type I ethylene interpolymer products (solid circles), the first ethylene interpolymer (single-site catalyst) and the second ethylene interpolymer (in-line Ziegler Natta catalyst) behave as a simple blend of two ethylene interpolymers and a hierarchical structure within the melt does not exist. However, in the case of Comparatives D and E (open diamonds), the melt comprising a first ethylene interpolymer (single-site catalyst) and a second ethylene interpolymer (batch Ziegler Natta catalyst) possesses a hierarchical structure.

The ethylene interpolymer products of this disclosure fall into one of two quadrants: Type I with X_(d)<0, or; Type II with X_(d)>0. The Dimensionless Modulus (X_(d)), reflects differences (relative to the reference sample) that are related to the overall molecular weight, molecular weight distribution (M_(w)/M_(n)) and short chain branching. Not wishing to be bound by theory, conceptually, the Dimensionless Modulus (X_(d)) may be considered to be related to the M_(w)/M_(n) and the radius of gyration (<R_(g)>²) of the ethylene interpolymer in the melt; conceptually, increasing X_(d) has similar effects as increasing M_(w)/M_(n) and/or <R_(g)>², without the risk of including lower molecular weight fraction and sacrificing certain related properties.

Relative to Comparative A (recall that Comparative A comprises a first and second ethylene interpolymer synthesized with a single-site catalyst) the solution process disclosed herein enables the manufacture of ethylene interpolymer products having higher X_(d). Not wishing to be bound by theory, as X_(d) increases the macromolecular coils of higher molecular weight fraction are more expanded (conceptually higher <R_(g)>²) and upon crystallization the probability of tie chain formation is increased resulting in higher toughness properties; the polyethylene art is replete with disclosures that correlate higher toughness (higher dad impact in manufactured film articles and improved ESCR and/or PENT in manufactured molding articles, e.g. containers and lids) with an increasing probability of tie chain formation.

In the Dilution Index testing protocol, the upper limit on Y_(d) may be about 20, in some cases about 15 and is other cases about 13. The lower limit on Y_(d) may be about −30, in some cases −25, in other cases −20 and in still other cases −15.

In the Dilution Index testing protocol, the upper limit on X_(d) is 1.0, in some cases about 0.95 and in other cases about 0.9. The lower limit on X_(d) is −2, in some cases −1.5 and in still other cases −1.0.

Terminal Vinyl Unsaturation of Ethylene Interpolymer Products

The ethylene interpolymer products of this disclosure are further characterized by a terminal vinyl unsaturation greater than or equal to 0.03 terminal vinyl groups per 100 carbon atoms (≧0.03 terminal vinyls/100 C); as determine via Fourier Transform Infrared (FTIR) spectroscopy according to ASTM D3124-98 and ASTM D6248-98.

FIG. 10 compares the terminal vinyl/100 C content of the ethylene interpolymers of this disclosure with several Comparatives. The data shown in FIG. 10 is also tabulated in Tables 11A and 11B. All of the comparatives in FIG. 10 and Tables 11A and 11B are Elite® products available from The Dow Chemical Company (Midland, Mich., USA); Elite products are ethylene interpolymers produced in a dual reactor solution process and comprise an interpolymer synthesized using a single-site catalyst and an interpolymer synthesized using a batch Ziegler-Natta catalyst: Comparative B is Elite 5401G; Comparative C is Elite 5400G; Comparative E and E2 are Elite 5500G; Comparative G is Elite 5960; Comparative H and H2 are Elite 5100G; Comparative I is Elite 5940G, and; Comparative J is Elite 5230G.

As shown in FIG. 10 the average terminal vinyl content in the ethylene interpolymer of this disclosure was 0.045 terminal vinyls/100 C; in contrast, the average terminal vinyl content in the Comparative samples was 0.023 terminal vinyls/100 C. Statistically, at the 99.999% confidence level, the ethylene interpolymers of this disclosure are significantly different from the Comparatives; i.e. a t-Test assuming equal variances shows that the means of the two populations (0.045 and 0.023 terminal vinyls/100 C) are significantly different at the 99.999% confidence level (t(obs)=12.891>3.510 t(crit two tail); or p-value=4.84×10⁻¹⁷<0.001 a (99.999% confidence)).

Catalyst Residues (Total Catalytic Metal)

The ethylene interpolymer products of this disclosure are further characterized by having ≧3 parts per million (ppm) of total catalytic metal (Ti); where the quantity of catalytic metal was determined by Neutron Activation Analysis (N.A.A.) as specified herein.

FIG. 11 compares the total catalytic metal content of the disclosed ethylene interpolymers with several Comparatives; FIG. 11 data is also tabulated in Tables 12A and 12B. All of the comparatives in FIG. 11 and Tables 12A and 12B are Elite® products available from The Dow Chemical Company (Midland, Mich., USA), for additional detail see the section above.

As shown in FIG. 11 the average total catalytic metal content in the ethylene interpolymers of this disclosure was 7.02 ppm of titanium; in contrast, the average total catalytic metal content in the Comparative samples was 1.63 ppm of titanium. Statistically, at the 99.999% confidence level, the ethylene interpolymers of this disclosure are significantly different from the Comparatives, i.e. a t-Test assuming equal variances shows that the means of the two populations (7.02 and 1.63 ppm titanium) are significantly different at the 99.999% confidence level, i.e. (t(obs)=12.71>3.520 t(crit two tail); or p-value=1.69×10⁻¹⁶<0.001α (99.999% confidence)).

Flexible Manufactured Articles

The ethylene interpolymer products disclosed herein, which are well suited to manufacture a wide variety of articles, have improved (higher) AHO melt strengths, improved (higher) heat deflection temperatures (HDT) and improved (shorter) half time of crystallization (t_(1/2)). Non-limiting examples include monolayer or multilayer films, such films are well known to those of ordinary experienced in the art. Non-limiting examples of processes to prepare such films include blown film and cast film processes.

Depending on the end-use application, the disclosed ethylene interpolymer products may be converted into films that span a wide range of thicknesses. Non-limiting examples include, food packaging films where thicknesses may range from about 0.5 mil (13 μm) to about 4 mil (102 μm), and; in heavy duty sack applications film thickness may range from about 2 mil (51 μm) to about 10 mil (254 μm).

The disclosed ethylene interpolymer products may be used in monolayer films; where the monolayer may contain more than one ethylene interpolymer product having improved color and/or additional thermoplastics; non-limiting examples of thermoplastics include ethylene polymers and propylene polymers. The lower limit on the weight percent of the ethylene interpolymer product having improved color in a monolayer film may be about 3 wt %, in other cases about 10 wt % and in still other cases about 30 wt %. The upper limit on the weight percent of the ethylene interpolymer product having improved color in the monolayer film may be 100 wt %, in other cases about 90 wt % and in still other cases about 70 wt %.

The ethylene interpolymer products disclosed herein may also be used in one or more layers of a multilayer film; non-limiting examples of multilayer films include three, five, seven, nine, eleven or more layers. The thickness of a specific layer (containing an ethylene interpolymer product having improved color) within a multilayer film may be about 5%, in other cases about 15% and in still other cases about 30% of the total multilayer film thickness. In other embodiments, the thickness of a specific layer (containing the ethylene interpolymer product having improved color) within a multilayer film may be about 95%, in other cases about 80% and in still other cases about 65% of the total multilayer film thickness. Each individual layer of a multilayer film may contain more than one ethylene interpolymer product and/or additional thermoplastics.

Additional embodiments include laminations and coatings, wherein mono or multilayer films containing the disclosed ethylene interpolymer products are extrusion laminated or adhesively laminated or extrusion coated. In extrusion lamination or adhesive lamination, two or more substrates are bonded together with a thermoplastic or an adhesive, respectively. In extrusion coating, a thermoplastic is applied to the surface of a substrate. These processes are well known to those experienced in the art.

In flexible applications there is a need to improve the melt strength of ethylene interpolymer products. The following are non-limiting examples. The rate at which blown film can be produced is frequently limited by bubble instability; higher melt strength ethylene interpolymer products have improved bubble stability which allows blown film production rates to be increased. Higher melt strength is also desired in thermoforming applications, where a film or sheet comprising an ethylene interpolymer product is heated and deformed by gravity (or gravity plus vacuum) into a mold, e.g. a tray or cup-like mold. Higher melt strength ethylene interpolymer products are also desired in foam applications, e.g. higher melt strengths are advantageous in producing lower density foams using chemical or physical blowing agents. Ethylene interpolymer products having higher heat deflection temperatures are desired in film applications; e.g. in the packaging of hot foods, or the cooking of foods within a film comprising a least one layer of an ethylene interpolymer product having a higher heat deflection temperature.

The ethylene interpolymer products disclosed herein can be used in a wide range of flexible manufactured articles, e.g. articles that comprise one or more films (monolayer or multilayer). In film applications, the disclosed ethylene interpolymer products are useful in food packaging applications. More specifically, the food packaging industry has a need for improved ethylene interpolymer products that can be converted into packaging films that have improved (reduced) water vapor transmission rate (WVTR). Low WVTR packaging film ensures that crackers are crispy when opened by the consumer; in addition, low WVTR films ensure that the packaged food has an acceptable shelf-life. The ethylene interpolymer products disclosed herein, may also be blended with nucleating agents. The term “nucleating agent” refers to any material that effectively accelerates the phase change from a molten ethylene interpolymer product to a solid semi-crystalline ethylene interpolymer product. Nucleating agents are frequently effective in reducing the WVTR of barrier films. Additional non-limiting examples where the disclosed ethylene interpolymers are useful in flexible manufactured articles include: fresh and frozen food packaging (including liquids, gels or solids), stand-up pouches, retortable packaging and bag-in-box packaging; barrier films (oxygen, moisture, aroma, oil, etc.) and modified atmosphere packaging; light and heavy duty shrink films and wraps, collation shrink film, pallet shrink film, shrink bags, shrink bundling and shrink shrouds; light and heavy duty stretch films, hand stretch wrap, machine stretch wrap and stretch hood films; high clarity films; heavy-duty sacks; household wrap, overwrap films and sandwich bags; industrial and institutional films, trash bags, can liners, magazine overwrap, newspaper bags, mail bags, sacks and envelopes, bubble wrap, carpet film, furniture bags, garment bags, coin bags, auto panel films; medical applications such as gowns, draping and surgical garb; construction films and sheeting, asphalt films, insulation bags, masking film, landscaping film and bags; geomembrane liners for municipal waste disposal and mining applications; batch inclusion bags; agricultural films, mulch film and green house films; in-store packaging, self-service bags, boutique bags, grocery bags, carry-out sacks and t-shirt bags; oriented films, machine direction and biaxially oriented films and functional film layers in oriented polypropylene (OPP) films, e.g. sealant and/or toughness layers. Additional manufactured articles comprising one or more films containing at least one ethylene interpolymer product having improved color include laminates and/or multilayer films; sealants and tie layers in multilayer films and composites; laminations with paper; aluminum foil laminates or laminates containing vacuum deposited aluminum; polyamide laminates; polyester laminates; extrusion coated laminates, and; hot-melt adhesive formulations. The manufactured articles summarized in this paragraph contain at least one film (monolayer or multilayer) comprising at least one embodiment of the disclosed ethylene interpolymer products.

Desired film physical properties (monolayer or multilayer) typically depend on the application of interest. Non-limiting examples of desirable film properties include: barrier properties (e.g. reducing water and oxygen transmission), optical properties (gloss, haze and clarity), dart impact, Elmendorf tear, modulus (1% and 2% secant modulus), puncture-propagation tear resistance, tensile properties (yield strength, break strength, elongation at break, toughness, etc.) and heat sealing properties (heat seal initiation temperature and hot tack strength). Specific hot tack and heat sealing properties are desired in high speed vertical and horizontal form-fill-seal processes that load and seal a commercial product (liquid, solid, paste, part, etc.) inside a pouch-like package.

Rigid Manufactured Articles

There is a need to improve the heat deflection temperature (HDT) of ethylene interpolymer products; such products with higher HDT are desired and valued in many applications, i.e. the molded part has a higher upper use temperature and is functional over a wider temperature range. Non-limiting examples of manufacture articles include containers and lids.

Additional non-limiting applications where the disclosed ethylene interpolymer may be used include: deli containers, margarine tubs, trays, cups, lids, bottles, bottle cap liners, pails, crates, drums, bumpers, industrial bulk containers, industrial vessels, material handling containers, playground equipment, recreational equipment, safety equipment, wire and cable applications (power cables, communication cables and conduits), tubing and hoses, pipe applications (pressure pipe and non-pressure pipe, e.g. natural gas distribution, water mains, interior plumbing, storm sewer, sanitary sewer, corrugated pipes and conduit), foamed articles (foamed sheet or bun foam), military packaging (equipment and ready meals), personal care packaging (diapers and sanitary products), cosmetic, pharmaceutical and medical packaging, truck bed liners, pallets and automotive dunnage. The rigid manufactured articles summarized in this paragraph contain one or more of the ethylene interpolymer products having improved heat deflection temperature (HDT), faster crystallization rate (reduced t_(1/2)) and higher melt strength. Such rigid manufactured articles may be fabricated using the conventional injection molding, compression molding and blow molding techniques.

The desired physical properties of rigid manufactured articles depend on the application of interest. Non-limiting examples of desired properties include: flexural modulus (1% and 2% secant modulus); tensile toughness; environmental stress crack resistance (ESCR); slow crack growth resistance (PENT); abrasion resistance; shore hardness; heat deflection temperature (HDT); VICAT softening point; IZOD impact strength; ARM impact resistance; Charpy impact resistance, and; color (whiteness and/or yellowness index).

A further objective of the present disclosure is to provide rigid manufactured articles comprising ethylene interpolymer products having improved heat deflection temperature, faster crystallization rate (reduced t_(1/2)) and improved (higher) melt strength that have improvements in at least one desirable physical property; relative to rigid manufactured articles formed from comparative ethylene interpolymers comprising ethylene interpolymers synthesized using a single-site catalyst.

Additives and Adjuvants

The ethylene interpolymer products and the manufactured articles described above may optionally include, depending on its intended use, additives and adjuvants. Non-limiting examples of additives and adjuvants include, anti-blocking agents, antioxidants, heat stabilizers, slip agents, processing aids, anti-static additives, colorants, dyes, filler materials, light stabilizers, heat stabilizers, light absorbers, lubricants, pigments, plasticizers, nucleating agents and combinations thereof. Non-limiting examples of suitable primary antioxidants include Irganox 1010 [CAS Reg. No. 6683-19-8] and Irganox 1076 [CAS Reg. No. 2082-79-3]; both available from BASF Corporation, Florham Park, N.J., U.S.A. Non-limiting examples of suitable secondary antioxidants include Irgafos 168 [CAS Reg. No. 31570-04-4], available from BASF Corporation, Florham Park, N.J., U.S.A.; Weston 705 [CAS Reg. No. 939402-02-5], available from Addivant, Danbury Conn., U.S.A. and; Doverphos Igp-11 [CAS Reg. No. 1227937-46-3] available form Dover Chemical Corporation, Dover Ohio, U.S.A.

Testing Methods

Prior to testing, each specimen was conditioned for at least 24 hours at 23±2° C. and 50±10% relative humidity and subsequent testing was conducted at 23±2° C. and 50±10% relative humidity. Herein, the term “ASTM conditions” refers to a laboratory that is maintained at 23±2° C. and 50±10% relative humidity; and specimens to be tested were conditioned for at least 24 hours in this laboratory prior to testing. ASTM refers to the American Society for Testing and Materials.

Density

Ethylene interpolymer product densities were determined using ASTM D792-13 (Nov. 1, 2013).

Melt Index

Ethylene interpolymer product melt index was determined using ASTM D1238 (Aug. 1, 2013). Melt indexes, I₂, I₆, I₁₀ and I₂₁ were measured at 190° C., using weights of 2.16 kg, 6.48 kg, 10 kg and a 21.6 kg respectively. Herein, the term “stress exponent” or its acronym “S.Ex.”, is defined by the following relationship:

S.Ex.=log(I ₆ /I ₂)/log(6480/2160)

wherein I₆ and I₂ are the melt flow rates measured at 190° C. using 6.48 kg and 2.16 kg loads, respectively. In this disclosure, melt index was expressed using the units of g/10 minutes or g/10 min or dg/minutes or dg/min; these units are equivalent.

Gel Permeation Chromatography (GPC)

Ethylene interpolymer product molecular weights, M_(n), M_(w) and M_(z), as well the as the polydispersity (M_(w)/M_(n)), were determined using ASTM D6474-12 (Dec. 15, 2012). This method illuminates the molecular weight distributions of ethylene interpolymer products by high temperature gel permeation chromatography (GPC). The method uses commercially available polystyrene standards to calibrate the GPC.

Isothermal Crystallization: Half Time of Crystallization (t_(1/2))

The isothermal crystallization rate of ethylene interpolymers were measured using a TA Instrument DSC Q2000 Thermal Analyser under a nitrogen atmosphere at 125.5° C. The interpolymer sample was first heated from ambient temperature to 150° C. at 20° C./min and kept at 150° C. for 10 minutes. Then the sample was cooled down to the crystallization temperature of interest (125.5° C.) at 70° C./min where the exothermic transition process was measured isothermally in terms of the heat flow and time. The half-time of crystallization (t_(1/2)) is defined as the time required for isothermal crystallization of 50 weight % of the interpolymer and determined from the area under the heat flow-time curve. The partial integral of the DSC crystallization curve represents the degree (or weight percentage) of crystallization at a given time and temperature.

Unsaturation Content

The quantity of unsaturated groups, i.e. double bonds, in an ethylene interpolymer product was determined according to ASTM D3124-98 (vinylidene unsaturation, published March 2011) and ASTM D6248-98 (vinyl and trans unsaturation, published July 2012). An ethylene interpolymer sample was: a) first subjected to a carbon disulfide extraction to remove additives that may interfere with the analysis; b) the sample (pellet, film or granular form) was pressed into a plaque of uniform thickness (0.5 mm), and; c) the plaque was analyzed by FTIR.

Comonomer Content

The quantity of comonomer in an ethylene interpolymer product was determined by FTIR (Fourier Transform Infrared spectroscopy) according to ASTM D6645-01 (published January 2010).

Composition Distribution Branching Index (CDBI)

The “Composition Distribution Branching Index” or “CDBI” of the disclosed Examples and Comparative Examples were determined using a crystal-TREF unit commercially available form Polymer ChAR (Valencia, Spain). The acronym “TREF” refers to Temperature Rising Elution Fractionation. A sample of ethylene interpolymer product (80 to 100 mg) was placed in the reactor of the Polymer ChAR crystal-TREF unit, the reactor was filled with 35 ml of 1,2,4-trichlorobenzene (TCB), heated to 150° C. and held at this temperature for 2 hours to dissolve the sample. An aliquot of the TCB solution (1.5 mL) was then loaded into the Polymer ChAR TREF column filled with stainless steel beads and the column was equilibrated for 45 minutes at 110° C. The ethylene interpolymer product was then crystallized from the TCB solution, in the TREF column, by slowly cooling the column from 110° C. to 30° C. using a cooling rate of 0.09° C. per minute. The TREF column was then equilibrated at 30° C. for 30 minutes. The crystallized ethylene interpolymer product was then eluted from the TREF column by passing pure TCB solvent through the column at a flow rate of 0.75 mL/minute as the temperature of the column was slowly increased from 30° C. to 120° C. using a heating rate of 0.25° C. per minute. Using Polymer ChAR software a TREF distribution curve was generated as the ethylene interpolymer product was eluted from the TREF column, i.e. a TREF distribution curve is a plot of the quantity (or intensity) of ethylene interpolymer eluting from the column as a function of TREF elution temperature. A CDBI₅₀ was calculated from the TREF distribution curve for each ethylene interpolymer product analyzed. The “CDBI₅₀” is defined as the percent of ethylene interpolymer whose composition is within 50% of the median comonomer composition (25% on each side of the median comonomer composition); it is calculated from the TREF composition distribution curve and the normalized cumulative integral of the TREF composition distribution curve. Those skilled in the art will understand that a calibration curve is required to convert a TREF elution temperature to comonomer content, i.e. the amount of comonomer in the ethylene interpolymer fraction that elutes at a specific temperature. The generation of such calibration curves are described in the prior art, e.g. Wild, et al., J. Polym. Sci., Part B, Polym. Phys., Vol. 20 (3), pages 441-455: hereby fully incorporated by reference.

Heat Deflection Temperature

The heat deflection temperature of an ethylene interpolymer product was determined using ASTM D648-07 (approved Mar. 1, 2007). The heat deflection temperature is the temperature at which a deflection tool applying 0.455 MPa (66 PSI) stress on the center of a molded ethylene interpolymer plaque (3.175 mm (0.125 in) thick) causes it to deflect 0.25 mm (0.010 in) as the plaque is heated in a medium at a constant rate.

Vicat Softening Point (Temperature)

The Vicat softening point of an ethylene interpolymer product was determined according to ASTM D1525-07 (published December 2009). This test determines the temperature at which a specified needle penetration occurs when samples are subjected to ASTM D1525-07 test conditions, i.e. heating Rate B (120±10° C./hr and 938 gram load (10±0.2N load).

Neutron Activation Analysis (NAA)

Neutron Activation Analysis, hereafter NAA, was used to determine catalyst residues in ethylene interpolymers and was performed as follows. A radiation vial (composed of ultrapure polyethylene, 7 mL internal volume) was filled with an ethylene interpolymer product sample and the sample weight was recorded. Using a pneumatic transfer system the sample was placed inside a SLOWPOKE™ nuclear reactor (Atomic Energy of Canada Limited, Ottawa, Ontario, Canada) and irradiated for 30 to 600 seconds for short half-life elements (e.g., Ti, V, Al, Mg, and Cl) or 3 to 5 hours for long half-life elements (e.g. Zr, Hf, Cr, Fe and Ni). The average thermal neutron flux within the reactor was 5×10¹¹/cm²/s. After irradiation, samples were withdrawn from the reactor and aged, allowing the radioactivity to decay; short half-life elements were aged for 300 seconds or long half-life elements were aged for several days. After aging, the gamma-ray spectrum of the sample was recorded using a germanium semiconductor gamma-ray detector (Ortec model GEM55185, Advanced Measurement Technology Inc., Oak Ridge, Tenn., USA) and a multichannel analyzer (Ortec model DSPEC Pro). The amount of each element in the sample was calculated from the gamma-ray spectrum and recorded in parts per million relative to the total weight of the ethylene interpolymer sample. The N.A.A. system was calibrated with Specpure standards (1000 ppm solutions of the desired element (greater than 99% pure)). One mL of solutions (elements of interest) were pipetted onto a 15 mm×800 mm rectangular paper filter and air dried. The filter paper was then placed in a 1.4 mL polyethylene irradiation vial and analyzed by the N.A.A. system. Standards are used to determine the sensitivity of the N.A.A. procedure (in counts/μg).

Color Index

The Whiteness Index (WI) and Yellowness Index (YI) of ethylene interpolymer products were measured according to ASTM E313-10 (approved in 2010) using a BYK Gardner Color-View colorimeter.

AHO Melt Strength

The Accelerated-Haul-Off (AHO) melt strength of ethylene interpolymer products were measured on a Rosand RH-7 capillary rheometer (available from Malvern Instruments Ltd, Worcestershire, UK) having a barrel diameter of 15 mm, a flat die of 2-mm diameter and L/D ratio of 10:1 and equipped with a pressure transducer of 10,000 psi (68.95 MPa). The polymer melt was extruded through a capillary die under a constant rate (constant piston speed of 5.33 mm/min at 190° C.) which formed an extruded polymer filament. The polymer filament was then passed through a set of rollers and stretched at an ever increasing haul-off speed until rupture. More specifically, the initial polymer filament speed was increased from 0 m/min at a constant acceleration rate from about 50 to 80 m/min² until the polymer filament ruptured. During this experiment, the force on the rollers was constantly measured, initially the force rises quickly and then plateaus prior to filament rupture. The maximum value of the force in the plateau region of the force versus time curve was defined as the melt strength for the polymer, measured in centi-Newtons (cN).

Dilution Index (Y_(d)) Measurements

A series of small amplitude frequency sweep tests were run on each sample using an Anton Paar MCR501 Rotational Rheometer equipped with the “TruGap™ Parallel Plate measuring system”. A gap of 1.5 mm and a strain amplitude of 10% were used throughout the tests. The frequency sweeps were from 0.05 to 100 rad/s at the intervals of seven points per decade. The test temperatures were 170°, 190°, 210° and 230° C. Master curves at 190° C. were constructed for each sample using the Rheoplus/32 V3.40 software through the Standard TTS (time-temperature superposition) procedure, with both horizontal and vertical shift enabled.

The Y_(d) and X_(d) data generated are summarized in Table 10. The flow properties of the ethylene interpolymer products, e.g., the melt strength and melt flow ratio (MFR) are well characterized by the Dilution Index (Y_(d)) and the Dimensionless Modulus (X_(d)) as detailed below. In both cases, the flow property is a strong function of Y_(d) and X_(d) in addition a dependence on the zero-shear viscosity. For example, the melt strength (hereafter MS) values of the disclosed Examples and the Comparative Examples were found to follow the same equation, confirming that the characteristic VGP point ((√{square root over (2)})G*_(c)/G*_(x), δ_(c)) and the derived regrouped coordinates (X_(d), Y_(d)) represent the structure well:

MS=a ₀₀ +a ₁₀ log η₀ −a ₂₀(90−δ_(c))−a ₃₀((√{square root over (2)})G* _(c) /G* _(x))−a ₄₀(90−δ_(c))((√{square root over (2)})G* _(c) /G* _(x))

where

-   -   a₀₀=−33.33; a₁₀=9.529; a₂₀=0.03517; a₃₀=0.894; a₄₀=0.02969 and         I²=0.984 and the average relative standard deviation was 0.85%.     -   Further, this relation can be expressed in terms of the Dilution         Index (Y_(d)) and the Dimensionless Modulus (X_(d)):

MS=a ₀ +a ₁ log η₀ +a ₂ Y _(d) +a ₃ X _(d) +a ₄ Y _(d) X _(d)

where

-   -   a₀=33.34; a₁=9.794; a₂=0.02589; a₃=0.1126; a₄=0.03307 and         r²=0.989 and the average relative standard deviation was 0.89%.

The MFR of the disclosed Examples and the Comparative samples were found to follow a similar equation, further confirming that the dilution parameters Y_(d) and X_(d) show that the flow properties of the disclosed Examples differ from the reference and Comparative Examples:

MFR=b ₀ −b ₁ log η₀ −b ₂ Y _(d) −b ₃ X _(d)

-   -   where     -   b₀=53.27; b₁=6.107; b₂=1.384; b₃=20.34 and r²=0.889 and the         average relative standard deviation and 3.3%.

Further, the polymerization process and catalyst formulations disclosed herein allow the production of ethylene interpolymer products that can be converted into flexible manufactured articles that have a desired balance of physical properties (i.e. several end-use properties can be balanced (as desired) through multidimensional optimization); relative to comparative polyethylenes of comparable density and melt index.

Dart Impact

Film dart impact strength was determined using ASTM D1709-09 Method A (May 1, 2009). In this disclosure the dart impact test employed a 1.5 inch (38 mm) diameter hemispherical headed dart.

Puncture

Film “puncture”, the energy (J/mm) required to break the film was determined using ASTM D5748-95 (originally adopted in 1995, reapproved in 2012).

Lubricated Puncture

The “lubricated puncture” test was performed as follows: the energy (J/mm) to puncture a film sample was determined using a 0.75-inch (1.9-cm) diameter pear-shaped fluorocarbon coated probe travelling at 10-inch per minute (25.4-cm/minute). ASTM conditions were employed. Prior to testing the specimens, the probe head was manually lubricated with Muko Lubricating Jelly to reduce friction. Muko Lubricating Jelly is a water-soluble personal lubricant available from Cardinal Health Inc., 1000 Tesma Way, Vaughan, ON L4K 5R8 Canada. The probe was mounted in an Instron Model 5 SL Universal Testing Machine and a 1000-N load cell as used. Film samples (1.0 mil (25 μm) thick, 5.5 inch (14 cm) wide and 6 inch (15 cm) long) were mounted in the Instron and punctured.

Tensile Properties

The following film tensile properties were determined using ASTM D882-12 (Aug. 1, 2012): tensile break strength (MPa), elongation at break (%), tensile yield strength (MPa), tensile elongation at yield (%) and film toughness or total energy to break (ft·lb/in³). Tensile properties were measured in the both the machine direction (MD) and the transverse direction (TD) of the blown films.

Film Modulus

The secant modulus is a measure of film stiffness. The secant modulus is the slope of a line drawn between two points on the stress-strain curve, i.e. the secant line. The first point on the stress-strain curve is the origin, i.e. the point that corresponds to the origin (the point of zero percent strain and zero stress), and; the second point on the stress-strain curve is the point that corresponds to a strain of 1%; given these two points the 1% secant modulus is calculated and is expressed in terms of force per unit area (MPa). The 2% secant modulus is calculated similarly. This method is used to calculated film modulus because the stress-strain relationship of polyethylene does not follow Hook's law; i.e. the stress-strain behavior of polyethylene is non-linear due to its viscoelastic nature. Secant moduli were measured using a conventional Instron tensile tester equipped with a 200 lbf load cell. Strips of monolayer film samples were cut for testing with following dimensions: 14 inch long, 1 inch wide and 1 mil thick; ensuring that there were no nicks or cuts on the edges of the samples. Film samples were cut in both the machine direction (MD) and the transverse direction (TD) and tested. ASTM conditions were used to condition the samples. The thickness of each film was accurately measured with a hand-held micrometer and entered along with the sample name into the Instron software. Samples were loaded in the Instron with a grip separation of 10 inch and pulled at a rate of 1 inch/min generating the strain-strain curve. The 1% and 2% secant modulus were calculated using the Instron software.

Flexural Properties

The flexural properties, i.e. flexural secant and tangent modulus and flexural strength were determined using ASTM D790-10 (published in April 2010).

Puncture-Propagation Tear

Puncture-propagation tear resistance of blown film was determined using ASTM D2582-09 (May 1, 2009). This test measures the resistance of a blown film to snagging, or more precisely, to dynamic puncture and propagation of that puncture resulting in a tear. Puncture-propagation tear resistance was measured in the machine direction (MD) and the transverse direction (TD) of the blown films.

Elmendorf Tear

Film tear performance was determined by ASTM D1922-09 (May 1, 2009); an equivalent term for tear is “Elmendorf tear”. Film tear was measured in both the machine direction (MD) and the transverse direction (TD) of the blown films.

Optical Properties

Film optical properties were measured as follows: Haze, ASTM D1003-13 (Nov. 15, 2013), and; Gloss ASTM D2457-13 (Apr. 1, 2013).

Dynatup Impact

Instrumented impact testing was carried out on a machine called a Dynatup Impact Tester purchased from Illinois Test Works Inc., Santa Barbara, Calif., USA; those skilled in the art frequently call this test the Dynatup impact test. Testing was completed according to the following procedure. Test samples are prepared by cutting about 5 inch (12.7 cm) wide and about 6 inch (15.2 cm) long strips from a roll of blown film; film was about 1 mil thick. Prior to testing, the thickness of each sample was accurately measured with a handheld micrometer and recorded. ASTM conditions were employed. Test samples were mounted in the 9250 Dynatup Impact drop tower/test machine using the pneumatic clamp. Dynatup tup #1, 0.5 inch (1.3 cm) diameter, was attached to the crosshead using the Allen bolt supplied. Prior to testing, the crosshead is raised to a height such that the film impact velocity is 10.9±0.1 ft/s. A weight was added to the crosshead such that: 1) the crosshead slowdown, or tup slowdown, was no more than 20% from the beginning of the test to the point of peak load and 2) the tup must penetrate through the specimen. If the tup does not penetrate through the film, additional weight is added to the crosshead to increase the striking velocity.

During each test the Dynatup Impulse Data Acquisition System Software collected the experimental data (load (lb) versus time). At least 5 film samples are tested and the software reports the following average values: “Dynatup Maximum (Max) Load (lb)”, the highest load measured during the impact test; “Dynatup Total Energy (ft·lb)”, the area under the load curve from the start of the test to the end of the test (puncture of the sample), and; “Dynatup Total Energy at Max Load (ft·lb)”, the area under the load curve from the start of the test to the maximum load point.

Hexane Extractables

Hexane extractables was determined according to the Code of Federal Registration 21 CFR §177.1520 Para (c) 3.1 and 3.2; wherein the quantity of hexane extractable material in a film is determined gravimetrically. Elaborating, 2.5 grams of 3.5 mil (89 μm) monolayer film was placed in a stainless steel basket, the film and basket were weighed (w^(i)), while in the basket the film was: extracted with n-hexane at 49.5° C. for two hours; dried at 80° C. in a vacuum oven for 2 hours; cooled in a desiccator for 30 minutes, and; weighed (w^(f)). The percent loss in weight is the percent hexane extractables (w^(C6)): w^(C6)=100×(w^(i)−w^(f))/w^(i).

Preparation of Nucleated Polymers

Embodiments of the ethylene interpolymer products were nucleated by adding 1200 ppm of Milliken HPN-20E additive (available from Milliken & Company, Spartanburg, S.C., USA); HPN-20E is a blend of a calcium and zinc salts of 1,2-cyclohexanedicarboxylkic acid. The HPN-20E was added to the ethylene interpolymer product by melt mixing on a Leistritz intermeshing co-rotating twin screw extruder with a screw diameter of 38 mm and a length to diameter ratio of 33/1. The extruder was operated at 205° C. at a screw speed and pelletizer speed of 120 rpm and about 40 to 45 rpm, respectively, under a nitrogen atmosphere. The output rate of the twin screw extruder was about 23 to 29 lb/hr.

Cast Film Production

Cast films of selected ethylene interpolymer products were manufactured using an OCS cast film line (available from OCS Optical Control Systems GmbH, Witten, Germany) which consisted of an extruder with a cast film die head and a chill roll and windup fixtures. A polymer sample was added into a 20 mm extruder with a mixing screw of 3:1 or 4:1 compression ratio and extruded at 40 rpm. The haul-off speed and chill roll temperature of the cast film line were set at 8.0 m/min and about 23 to 30° C., respectively. The temperature profile for the cast film extruder was 210° C. in the feed region and 220° C. in the die and extruder barrel. The cast films produced were 1.5 mil thick and from about 3.0 to 5.0 inches wide; the physical properties these cast films were determined as described above.

Water Vapor Transmission Rate (WVTR)

Water Vapor Transmission Rate (WVTR), expressed as grams of water vapor transmitted per 100 square inches of film per day at a specified film thickness (mils), or g/100 in²/day) was measured in accordance with ASTM F1249-90 with a MOCON Permatron available from Modern Controls Inc. at conditions of 100° F. (37.8° C.) and 100% relative humidity. A control (comparative) experiment was conducted using a single low melt index HDPE resin having a melt index of about 0.95 grams/10 minutes, a density of 0.9575 g/cc and a molecular weight distribution, M_(w)/M_(n), of 3.51 (an ethylene homopolymer designated SCLAIR™ 19C (available from NOVA Chemicals Inc., Calgary, Alberta, Canada). The WVTR test was run in duplicate and the average WVTR was reported.

Oxygen Transmission Rate (OTR)

Oxygen transmission rate (OTR), expressed as cm³ of oxygen transmitted per 100 square inches of film per day at a specified film thickness (mils), or cm³/100 in²/day) was measured on film samples (4 inch×4 inch) at 0% relative humidity and 23° C. using MOCON OXTRAN System Model 2/21T. The OTR test was run in duplicate and the average rate of oxygen permeation was determined at an equilibrium state.

Examples Polymerization

The following examples are presented for the purpose of illustrating selected embodiments of this disclosure; it being understood, that the examples presented do not limit the claims presented.

Embodiments of ethylene interpolymer product having improved heat deflection temperature (HDT), faster crystallization rate (lower t_(1/2)) and improved melt strength were produced in a continuous solution polymerization pilot plant comprising reactors arranged in a series configuration. Methylpentane was used as the process solvent (a commercial blend of methylpentane isomers). The volume of the first CSTR reactor (R1) was 3.2 gallons (12 L), the volume of the second CSTR reactor (R2) was 5.8 gallons (22 L) and the volume of the tubular reactor (R3) was 4.8 gallons (18 L). Examples of ethylene interpolymer products were produced using an R1 pressure from about 14 MPa to about 18 MPa; R2 was operated at a lower pressure to facilitate continuous flow from R1 to R2. R1 and R2 were operated in series mode, wherein the first exit stream from R1 flows directly into R2. Both CSTR's were agitated to give conditions in which the reactor contents were well mixed. The process was operated continuously by feeding fresh process solvent, ethylene, 1-octene and hydrogen to the reactors.

The single site catalyst components used were: component (i), cyclopentadienyl tri(tertiary butyl)phosphinimine titanium dichloride, (Cp[(t-Bu)3PN]TiCl₂), hereafter PIC-1; component (ii), methylaluminoxane (MAO-07); component (iii), trityl tetrakis(pentafluoro-phenyl)borate, and; component (iv), 2,6-di-tert-butyl-4-ethylphenol. The single site catalyst component solvents used were methylpentane for components (ii) and (iv) and xylene for components (i) and (iii). The quantity of PIC-1 added to R1, “R1 (i) (ppm)” is shown in Table 2A; to be clear, in Example 20 in Table 2A, the solution in R1 contained 0.12 ppm of component (i), i.e. PIC-1. The mole ratios of the single site catalyst components employed to produce Example 20 were: R1 (ii)/(i) mole ratio=100, i.e. [(MAO-07)/(PIC-1)]; R1 (iv)/(ii) mole ratio=0.07, i.e. [(2,6-di-tert-butyl-4-ethylphenol)/(MAO-07)], and; R1 (iii)/(i) mole ratio=1.1, i.e. [(trityl tetrakis(pentafluoro-phenyl)borate)/(PIC-1)]. The single site catalyst formulation was injected into R1 using process solvent, the flow rate of this catalyst containing solvent was about 30 kg/hr.

The in-line Ziegler-Natta catalyst formulation was prepared from the following components: component (v), butyl ethyl magnesium; component (vi), tertiary butyl chloride; component (vii), titanium tetrachloride; component (viii), diethyl aluminum ethoxide, and; component (ix), triethyl aluminum.

Methylpentane was used as the catalyst component solvent. The in-line Ziegler-Natta catalyst formulation was prepared using the following steps. In step one, a solution of triethylaluminum and dibutylmagnesium ((triethylaluminum)/(dibutylmagnesium) molar ratio of 20) was combined with a solution of tertiary butyl chloride and allowed to react for about 30 seconds (HUT-1); in step two, a solution of titanium tetrachloride was added to the mixture formed in step one and allowed to react for about 14 seconds (HUT-2), and; in step three, the mixture formed in step two was allowed to reactor for an additional 3 seconds (HUT-3) prior to injection into R2. The in-line Ziegler-Natta procatalyst formulation was injected into R2 using process solvent, the flow rate of the catalyst containing solvent was about 49 kg/hr. The in-line Ziegler-Natta catalyst formulation was formed in R2 by injecting a solution of diethyl aluminum ethoxide into R2. The quantity of titanium tetrachloride “R2 (vii) (ppm)” added to reactor 2 (R2) is shown in Table 2A; to be clear in Example 20 the solution in R2 contained 5.23 ppm of TiCl₄. The mole ratios of the in-line Ziegler-Natta catalyst components are also shown in Table 2A, specifically: R2 (vi)/(v) mole ratio, i.e. [(tertiary butyl chloride)/(butyl ethyl magnesium)]; R2 (viii)/(vii) mole ratio, i.e. [(diethyl aluminum ethoxide)/(titanium tetrachloride)], and; R2 (ix)/(vii) mole ratio, i.e. [(triethyl aluminum)/(titanium tetrachloride)]. To be clear, in Example 20, the following mole ratios were used to synthesize the in-line Ziegler-Natta catalyst: R2 (vi)/(v) mole ratio=1.75; R2 (viii)/(vii) mole ratio=1.35, and; R2 (ix)/(vii) mole ratio=0.35. In all of the Examples disclosed, 100% of the diethyl aluminum ethoxide was injected directly into R2.

In Comparative Example 10, a single site catalyst formulation was employed in both reactor 1 and reactor 2. Relative to Comparative Example 10, the maximum ethylene interpolymer product production rates (kg/h) of Examples 20-24, in which a single-site catalyst formulation was used in R1 and a heterogeneous catalyst formulation was used in R2, were at least 23% higher. For example, in Example 20 (single-site catalyst formulation in R1+in-line Ziegler-Natta catalyst in R2) the ethylene interpolymer product was produced at a production rate of 93.1 kg/h; in contrast, in Comparative Example 10 (single-site catalyst formulation in both R1 and R2) the maximum production rate of the comparative ethylene interpolymer product was 75.8 kg/h.

Average residence time of the solvent in a reactor is primarily influenced by the amount of solvent flowing through each reactor and the total amount of solvent flowing through the solution process, the following are representative or typical values for the examples shown in Tables 2A-2C: average reactor residence times were: about 61 seconds in R1, about 73 seconds in R2 and about 50 seconds in R3 (the volume of R3 was about 4.8 gallons (18L)).

Polymerization in the continuous solution polymerization process was terminated by adding a catalyst deactivator to the third exit stream exiting the tubular reactor (R3). The catalyst deactivator used was octanoic acid (caprylic acid), commercially available from P&G Chemicals, Cincinnati, Ohio, U.S.A. The catalyst deactivator was added such that the moles of fatty acid added were 50% of the total molar amount of titanium and aluminum added to the polymerization process; to be clear, the moles of octanoic acid added=0.5×(moles titanium+moles aluminum); this mole ratio was consistently used in all examples.

A two-stage devolitizing process was employed to recover the ethylene interpolymer product from the process solvent, i.e. two vapor/liquid separators were used and the second bottom stream (from the second V/L separator) was passed through a gear pump/pelletizer combination. DHT-4V (hydrotalcite), supplied by Kyowa Chemical Industry Co. LTD, Tokyo, Japan was used as a passivator, or acid scavenger, in the continuous solution process. A slurry of DHT-4V in process solvent was added prior to the first V/L separator. The molar amount of DHT-4V added was about 10-fold higher than the molar amount of chlorides added to the process; the chlorides added were titanium tetrachloride and tertiary butyl chloride.

Prior to pelletization the ethylene interpolymer product was stabilized by adding about 500 ppm of Irganox 1076 (a primary antioxidant) and about 500 ppm of Irgafos 168 (a secondary antioxidant), based on weight of the ethylene interpolymer product. Antioxidants were dissolved in process solvent and added between the first and second V/L separators.

Tables 2B and 2C disclose additional solution process parameters, e.g. ethylene and 1-octene splits between the reactors, reactor temperatures and ethylene conversions, etc. recorded during the production of Examples 20-24 and Comparative Example 10. In Tables 2A-2C the targeted ethylene interpolymer product was 1.2 melt index (12) (ASTM D1239, 2.16 kg load, 190° C.) and 0.962 g/cc (ASTM D792). In Comparative Example 10, the single-site catalyst formulation was injected into both reactor R1 and reactor R2 and ES^(R1) was 45%. In Example 20, the single site catalyst formulation was injected into R1, the in-line Ziegler-Natta catalyst formulation was injected into R2 and ESR1 was 45%. Based on catalyst flows the total catalytic metal in Example 20-24 varied from about 5.2 ppm to about 6.4 ppm of titanium.

TABLE 1 Computer generated Simulated Example 13: single-site catalyst formulation in R1 (PIC-1) and an in-line Ziegler-Natta catalyst formulation in R2 and R3. Reactor 1 Reactor 2 Reactor 3 Simu- Simulated (R1) First (R2) Second (R3) Third lated Physical Ethylene Ethylene Ethylene Example Property Interpolymer Interpolymer Interpolymer 13 Weight 36.2 56.3 7.5 100 Percent (%) M_(n) 63806 25653 20520 31963 M_(w) 129354 84516 67281 99434 M_(z) 195677 198218 162400 195074 Poly- 2.03 3.29 3.28 3.11 dispersity (M_(w)/M_(n)) Branch 12.6 11.4 15.6 12.1 Frequency (C₆ Branches per 1000 C.) CDBI₅₀ (%) 90 to 95 55 to 60 45 to 55 65 to 70 (range) Density 0.9087 0.9206 0.9154 0.9169 (g/cm³) Melt Index 0.31 1.92 4.7 1.0 (dg/min)

TABLE 2A Continuous solution process catalyst parameters for: Examples 20-24 and Comparative Example 10, targeting ethylene interpolymer products at 1.2 I₂ and 0.962 g/cm³. Comparative Sample Code Example 20 Example 21 Example 22 Example 23 Example 24 Example 10 R1 Catalyst PIC-1 PIC-1 PIC-1 PIC-1 PIC-1 PIC-1 R2 Catalyst ZN ZN ZN ZN ZN PIC-1 R1 (i) (ppm) 0.12 0.10 0.09 0.11 0.07 0.11 R1 (ii)/(i) mole ratio 100    100 100 100.1 99.9 100 R1 (iv)/(ii) mole ratio 0.07 0.1 0.1 0.08 0.20 0.30 R1 (iii)/(i) mole ratio 1.1  1.1 1.1 1.1 1.1 1.1 R2 (i) (ppm) 0   0 0 0 0 0.44 R2 (ii)/(i) mole ratio 0   0 0 0 0 25 R2 (iv)/(ii) mole ratio 0   0 0 0 0 0.30 R2 (iii)/(i) mole ratio 0   0 0 0 0 1.20 R2 (vii) (ppm) 5.23 6.21 6.38 6.18 5.71 0 R2 (vi)/(v) mole ratio 1.75 1.75 1.75 1.75 1.75 0 R2 (viii)/(vii) mole ratio 1.35 1.35 1.35 1.35 1.34 0 R2 (ix)/(vii) mole ratio 0.35 0.35 0.35 0.36 0.35 0 Prod. Rate (kg/h) 93.1  95.6 97.6 97.5 99.4 75.8 Increase in Prod. Rate (%) 23^(a)   26 29 29 31 ^(a)For example: Increase in Prod. Rate (%) = 23% = 100(93.1 − 75.8)/75.8

TABLE 2B Additional solution process parameters for Examples 20-24 and Comparative Example 10. Comparative Appln Code Example 20 Example 21 Example 22 Example 23 Example 24 Example 10 R3 volume (L) 18 18 18 18 18 18 ES^(R1) (%) 45 45 35 35 20 45 ES^(R2) (%) 55 55 65 65 80 55 ES^(R3) (%) 0 0 0 0 0 0 R1 ethylene concentration 10.8 10.8 10.8 10.59 9.19 10.8 (wt %) R2 ethylene concentration 16.5 16.9 17.3 17.3 17.9 14.1 (wt %) R3 ethylene concentration 16.5 16.9 17.3 17.3 17.9 14.1 (wt %) ((octene)/(ethylene)) in R1 0 0 0 0 0 0 (wt %) OS^(R1) (%) 0 0 0 0 0 0 OS^(R2) (%) 0 0 0 0 0 0 OS^(R3) (%) 0 0 0 0 0 0 H₂ ^(R1) (ppm) 1.7 1.15 0.51 0.23 0.26 1.0 H₂ ^(R2) (ppm) 40.0 82.0 82.0 82.1 82.1 40 H₂ ^(R3) (ppm) 0 0 0 0 0 0 Prod. Rate (kg/h) 93.1 95.6 97.6 97.5 99.4 75.8 Increase in Prod. Rate (%) 23 26 29 29 31 ^(a) For example: Increase in Prod. Rate (%) = 23% = 100(93.1 − 75.8)/75.8

TABLE 2C Additional solution process parameters for Examples 20-24 and Comparative Example 10. Comparative Code Example 20 Example 21 Example 22 Example 23 Example 24 Example 10 R1 total solution rate (kg/h) 412.3 422.6 336.6 342.5 233.8 350.4 R2 total solution rate (kg/h) 186.8 177.6 263.5 257.4 366.5 249.6 R3 solution rate (kg/h) 0 0 0 0 0 0 Overall total solution rate (kg/h) 599.1 600.1 600.1 599.9 600.3 600.0 R1 inlet temp (° C.) 30.3 30.6 29.5 29.9 30.2 30.0 R2 inlet temp (° C.) 30.5 29.8 29.7 29.8 30.1 30.0 R3 inlet temp(° C.) 130 130 130 130 130 130 R1 Mean temp (° C.) 163 163.5 163.0 161.9 145.5 163.0 R2 Mean temp (° C.) 214.6 220.5 220 220 219.7 193.0 R3 exit temp (actual) (° C.) 221.2 225.2 227.3 227.1 229 195.9 R3 exit temp (calc) (° C.) 224.3 229.5 232.6 232.3 235.6 195.9 Q^(R1) (%) 93.6 93.6 93.4 94.0 92.9 93.5 Q^(R2) (%) 79.8 80.2 80.8 80.4 n/a¹ 77.2 Q^(R2+R3) (%) 89.8 90.2 91.3 90.9 90.7 82.5 Q^(R3) (%) 49.3 50.3 54.5 53.5 n/a¹ 23.4 Q^(T) (%) 94.1 94.3 94.1 93.9 92.4 89.9 Prod. Rate (kg/h) 93.1 95.6 97.6 97.5 99.4 75.8 Increase in Prod. Rate (%) 23 26 29 29 31 ^(a) For example: Increase in Prod. Rate (%) = 23% = 100(93.1 − 75.8)/75.8 ¹fouled probe

TABLE 3 Examples 20-24 and Comparative Example 10 and Comparative F. Melt Index Density I₂ (g/10 Melt Flow Ratio Stress Code (g/cm³) min) (I₂₁/I₂) Exponent Mw Mz Mw/Mn Example 20 0.9596 1.21 31.3 1.35 106790 283265 3.19 Example 21 0.9618 1.31 38.3 1.39 98550 250975 3.80 Example 22 0.9620 1.3 51.0 1.49 99091 296077 4.23 Example 23 0.9621 0.63 78.9 1.68 125350 527430 5.99 Example 24 0.9646 1.98 83.0 1.79 95918 425777 5.27 Comparative 0.9644 1.20 63.0 1.43 102131 340866 9.25 Example 10

TABLE 4 Accelerated Haul Off (AHO) Melt Strength of Examples 20-24 relative to Comparative Examples G1-G8; Comparative Examples G1-G8 are eight samples of the commercial resin HPs167-AB. Melt Index (I₂) AHO Melt Sample Code dg/min Strength (cN) Example 23 0.63 4.88 Example 22 1.21 3.16 Example 20 1.3 3.15 Example 21 1.31 2.99 Example 24 1.98 2.58 Comparative G1 1.1 2.92 Comparative G2 1.11 2.62 Comparative G3 1.12 2.55 Comparative G4 1.17 2.7 Comparative G5 1.18 2.73 Comparative G6 1.18 2.98 Comparative G7 1.2 2.46 Comparative G8 1.22 2.63

TABLE 5 Influence of nucleation and melt flow properties (melt index (MI or I₂) and melt flow ratio (MFR or (I₂₁/I₂)) on resin density. Density MI or I₂ MFR ((2225/ Sample Code (g/cc) (dg/min) (I₂₁/I₂) MFR²) − MI) Example 20 0.9596 1.21 31.3 1.0611 Example 21 0.9618 1.31 38.3 0.2068 Example 22 0.9620 1.3 51 −0.4446 Example 23 0.9621 0.63 78.9 −0.2726 Example 24 0.9646 1.98 83 −1.6570 Example 20* 0.9621 1.24 31.3 1.0311 Example 21* 0.9631 1.28 37.9 0.2690 Example 22* 0.9646 1.29 51 −0.4346 Example 23* 0.9648 0.65 77 −0.2747 Example 24* 0.9665 1.97 83 −1.6470 *Sample contains 1200 ppm of nucleator

TABLE 6 Half time of crystallization (t_(1/2)) of Examples 20-24 and Comparative Example 10; isothermal crystallization at 125.5° C. Half Time Of Crystallization at 125.5° C.; t_(1/2) (min) Un-nucleated Nucleated¹ Resin Samples Samples Example 20 8.04 1.67 Example 21 13.5 1.77 Example 22 9.92 1.71 Example 23 10.5 1.84 Example 24 7.53 1.65 Average of Examples 20-24 9.91 ± 2.38 1.73 ± 0.08 Comparative Example 10 51.6 3.09 ¹samples contain 1200 ppm of the nucleating agent HPN-20E (a blend of calcium and zinc salts of 1,2-cyclohexanedicarboxylkic acid).

TABLE 7 Heat deflection temperature (HDT, ° C.) measured according to ASTM D648-07, of Examples 20-24 and Comparative Example 10. Density MI or I₂ Heat Deflection Sample Code (g/cc) (dg/min) Temperature (° C.) Example 20 0.9596 1.21 79.0 Example 21 0.9618 1.31 74.0 Example 22 0.9620 1.30 81.8 Example 23 0.9621 0.63 79.7 Example 24 0.9646 1.98 85.1 Comp. Ex. 10 0.9644 1.20 78.7 Example 20* 0.9621 1.24 81.6 Example 21* 0.9631 1.28 85.0 Example 22* 0.9646 1.29 84.3 Example 23* 0.9648 0.65 83.0 Example 24* 0.9665 1.97 87.0 Comp. Ex. 10* 0.9660 1.22 78.3 *Sample contains 1200 ppm of nucleator

TABLE 8 Un-nucleated film properties (1.5 mil film) of Examples 20-24 and Comparative Example 10. Comp. Sample Code Example 20 Example 21 Example 22 Example 23 Example 24 Ex. 10 WVTR (g · mil/100 in²/day · atm) 0.3558 0.3938 0.4284 0.5856 0.4563 0.3324 OTR (cm³ · mil/ 106.6 163.6 173.5 258.2 384.1 476.8 100 in²/day · atm) Slow Puncture Lube/Tef (J/mm) n/a n/a n/a n/a 20 26 Dynatup Film Max Load (lb) n/a n/a 3.68 3.45 3.67 3.74 Dynatup Total Energy (Ftlb) n/a n/a 0.06 0.05 0.05 0.06 Dynatup Energy at Max Load n/a n/a 0.03 0.03 0.03 0.04 (Ftlb) 1% Sec Modulus - MD (Mpa) 614 478 772 738 723 815 2% Sec Modulus - MD (Mpa) 510 443 648 623 595 642 Tensile Break Str - MD (Mpa) 44.3 49.3 48.1 65.2 49.6 64.4 Elongation at Break - MD (%) 702 705 674 565 706 723 Tensile Yield Str - MD (Mpa) 21.7 25 26.5 27.3 26.6 29.6 Tensile Elong at Yield - MD (%) 10 9 9 8 8 8 GLOSS 45 67 66 52 21 46 52 HAZE 12.1 11.9 14.4 38.8 22.6 23.3 Hexane Extractables¹ 0.09 0.22 0.21 0.16 0.20 0.40 ¹Generated from a molded plaque sample

TABLE 9 Nucleated film properties (1.5 mil film) of Examples 20-24 and Comparative Example 10. Comp. Sample Code Example 20 Example 21 Example 22 Example 23 Example 24 Ex. 10 WVTR (g · mil/100 in²/day · atm) 0.3467 0.3257 0.3477 0.6015 0.3642 0.1706 OTR (cm³ · mil/ 316.3 303.3 250.3 344.6 296.0 186.4 100 in²/day · atm) Slow Puncture Lube/Tef 17 17 19 25 18 20 (J/mm) Dynatup Film Max Load (lb) 3.41 3.5 3.36 3.54 3.29 2.54 Dynatup Total Energy (Ftlb) 0.06 0.07 0.05 0.06 0.04 0.04 Dynatup Energy at Max Load 0.03 0.03 0.03 0.03 0.03 0.02 (Ftlb) 1% Sec Modulus - MD (Mpa) 538 623 588 680 704 668 2% Sec Modulus - MD (Mpa) 461 525 533 589 578 576 Tensile Break Str - MD (Mpa) 48.1 52.6 64.3 66.1 54.6 54.1 Elongation at Break - MD (%) 769 732 794 536 773 704 Tensile Yield Str - MD (Mpa) 22.3 25 28.6 28.3 26.2 28.4 Tensile Elong at Yield - MD 11 9 9 8 8 9 (%) GLOSS 45 73 69 64 21 44 60 HAZE 10.4 9.8 12.5 33.0 19.8 13.7

TABLE 10 Dilution Index (Y_(d)) and Dimensionless Modulus Data (X_(d)) for selected embodiments of ethylene interpolymers of this disclosure (Examples), relative to Comparative S, A, D and E. Density MI MS η₀ G⁰ _(N) G*_(c) δ_(c) Sample Code [g/cm³] [dg/min] MFR [cN] [kPa · s] [MPa] [kPa] [°] X_(d) Y_(d) Comp. S 0.9176 0.86 29.2 6.46 11.5 1.50 9.43 74.0 0.00 0.02 Comp. A 0.9199 0.96 29.6 5.99 10.6 1.17 5.89 80.1 −0.20 3.66 Example 6 0.9152 0.67 23.7 7.05 12.9 1.57 7.89 79.6 −0.08 4.69 Example 101 0.9173 0.95 26.3 5.73 9.67 0.84 7.64 79.0 −0.09 3.93 Example 102 0.9176 0.97 22.6 5.65 9.38 1.46 7.46 79.5 −0.10 4.29 Example 103 0.9172 0.96 25.3 5.68 9.38 1.44 7.81 79.3 −0.08 4.29 Example 110 0.9252 0.98 23.9 5.57 9.41 1.64 8.90 78.1 −0.03 3.8 Example 115 0.9171 0.75 23.4 6.83 12.4 1.48 8.18 79.2 −0.06 4.44 Example 200 0.9250 1.04 24.2 5.33 8.81 0.97 8.97 78.9 −0.02 4.65 Example 201 0.9165 1.01 27.1 5.43 8.75 0.85 6.75 79.7 −0.15 3.91 Example 120 0.9204 1.00 24.0 5.99 10.2 1.45 13.5 73.6 0.16 1.82 Example 130 0.9232 0.94 22.1 6.21 10.4 0.97 11.6 75.7 0.09 3.02 Example 131 0.9242 0.95 22.1 6.24 10.7 1.02 11.6 75.3 0.09 2.59 Comp. D 0.9204 0.82 30.6 7.61 15.4 1.58 10.8 70.4 0.06 −2.77 Comp. E 0.9161 1.00 30.5 7.06 13.8 1.42 10.4 70.5 0.04 −2.91 (MFR = melt flow rate (I₂₁/I₂); MS = melt strength)

TABLE 11A Unsaturation data of several embodiments of the disclosed ethylene interpolymers, as well as Comparative B, C, E, E2, G, H, H2, I and J; as determined by ASTM D3124-98 and ASTM D6248-98. Density Melt Index Melt Flow Stress Unsaturations per 100 C. Sample Code (g/cm³) I₂ (dg/min) Ratio (I₂₁/I₂) Exponent Internal Side Chain Terminal Example 11 0.9113 0.91 24.8 1.24 0.009 0.004 0.037 Example 6 0.9152 0.67 23.7 1.23 0.008 0.004 0.038 Example 4 0.9154 0.97 37.1 1.33 0.009 0.004 0.047 Example 7 0.9155 0.70 25.7 1.24 0.008 0.005 0.042 Example 2 0.9160 1.04 27.0 1.26 0.009 0.005 0.048 Example 5 0.9163 1.04 25.9 1.23 0.008 0.005 0.042 Example 3 0.9164 0.9 29.2 1.27 0.009 0.004 0.049 Example 53 0.9164 0.9 29.2 1.27 0.009 0.004 0.049 Example 51 0.9165 1.01 28.0 1.26 0.009 0.003 0.049 Example 201 0.9165 1.01 27.1 1.22 0.008 0.007 0.048 Example 1 0.9169 0.88 23.4 1.23 0.008 0.005 0.044 Example 52 0.9169 0.85 29.4 1.28 0.008 0.002 0.049 Example 55 0.9170 0.91 29.8 1.29 0.009 0.004 0.050 Example 115 0.9171 0.75 23.4 1.22 0.007 0.003 0.041 Example 43 0.9174 1.08 24.2 1.23 0.007 0.007 0.046 Comparative E2 0.9138 1.56 24.1 1.26 0.006 0.007 0.019 Comparative E 0.9144 1.49 25.6 1.29 0.004 0.005 0.024 Comparative J 0.9151 4.2 21.8 1.2 0.006 0.002 0.024 Comparative C 0.9161 1 30.5 1.35 0.004 0.004 0.030 Comparative B 0.9179 1.01 30.2 1.33 0.004 0.002 0.025 Comparative H2 0.9189 0.89 30.6 1.36 0.004 0.002 0.021 Comparative H 0.9191 0.9 29.6 1.34 0.004 0.003 0.020 Comparative I 0.9415 0.87 62 1.61 0.002 0.000 0.025 Comparative G 0.9612 0.89 49 1.58 0.000 0.000 0.023

TABLE 11B Additional unsaturation data of several embodiments of the disclosed ethylene interpolymers; as determined by ASTM D3124-98 and ASTM D6248-98. Density Melt Index Melt Flow Unsaturations per 100 C. Sample Code (g/cm³) I₂ (dg/min) Ratio (I₂₁/I₂) S. Ex. Internal Side Chain Terminal Example 8 0.9176 4.64 27.2 1.25 0.009 0.001 0.048 Example 42 0.9176 0.99 23.9 1.23 0.007 0.006 0.046 Example 102 0.9176 0.97 22.6 1.24 0.007 0.005 0.044 Example 54 0.9176 0.94 29.9 1.29 0.009 0.002 0.049 Example 41 0.9178 0.93 23.8 1.23 0.007 0.006 0.046 Example 44 0.9179 0.93 23.4 1.23 0.007 0.007 0.045 Example 9 0.9190 0.91 40.3 1.38 0.008 0.003 0.052 Example 200 0.9250 1.04 24.2 1.24 0.006 0.005 0.050 Example 60 0.9381 4.57 22.2 1.23 0.005 0.002 0.053 Example 61 0.9396 4.82 20.2 1.23 0.002 0.002 0.053 Example 62 0.9426 3.5 25.4 1.26 0.002 0.002 0.052 Example 70 0.9468 1.9 32.3 1.34 0.001 0.002 0.042 Example 71 0.9470 1.61 34.8 1.35 0.001 0.001 0.048 Example 72 0.9471 1.51 31.4 1.34 0.001 0.002 0.043 Example 73 0.9472 1.51 31.6 1.35 0.001 0.002 0.047 Example 80 0.9528 1.53 41.1 1.38 0.002 0.000 0.035 Example 81 0.9533 1.61 50 1.43 0.002 0.000 0.044 Example 82 0.9546 1.6 59.6 1.5 0.001 0.000 0.045 Example 90 0.9588 7.51 29 1.28 0.001 0.000 0.042 Example 91 0.9589 6.72 30.4 1.29 0.002 0.000 0.041 Example 20 0.9596 1.21 31.3 1.35 0.002 0.001 0.036 Example 21 0.9618 1.31 38.3 1.39 0.002 0.001 0.037 Example 22 0.9620 1.3 51 1.49 0.002 0.001 0.041 Example 23 0.9621 0.63 78.9 1.68 0.002 0.001 0.042 Example 24 0.9646 1.98 83 1.79 0.001 0.001 0.052

TABLE 12A Neutron Activation Analysis (NAA) catalyst residues in several embodiments of the disclosed ethylene interpolymers, as well as Comparatives G, I, J, B, C, E, E2, H and H2. N.A.A. Elemental Density Melt Index Analysis (ppm) Sample Code (g/cm³) I₂ (dg/min) Ti Mg Cl Al Example 60 0.9381 4.57 9.0 140 284 127 Example 62 0.9426 3.50 9.2 179 358 94 Example 70 0.9468 1.90 6.2 148 299 99 Example 71 0.9470 1.61 6.8 168 348 87 Example 72 0.9471 1.51 5.8 178 365 88 Example 73 0.9472 1.51 7.2 142 281 66 Example 80 0.9528 1.53 4.3 141 288 82 Example 81 0.9533 1.61 6.4 163 332 82 Example 82 0.9546 1.60 5.8 132 250 95 Example 90 0.9588 7.51 6.7 143 286 94 Example 91 0.9589 6.72 6.7 231 85 112 Example 1 0.9169 0.88 6.1 199 99 97 Example 2 0.9160 1.04 7.4 229 104 112 Example 3 0.9164 0.90 7.3 268 137 129 Comparative G 0.9612 0.89 1.6 17.2 53 11 Comparative I 0.9415 0.87 2.3 102 24 53 Comparative J 0.9151 4.20 1.4 <2 0.6 7.9 Comparative B 0.9179 1.01 0.3 13.7 47 9.3 Comparative C 0.9161 1.00 2.0 9.0 25 5.4 Comparative E2 0.9138 1.56 1.2 9.8 32.2 6.8 Comparative E 0.9144 1.49 1.3 14.6 48.8 11.3 Comparative H 0.9191 0.90 2.2 14.6 48.8 11.3 Comparative H2 0.9189 0.89 2.2 253 122 130

TABLE 12B Additional Neutron Activation Analysis (NAA) catalyst residues in several embodiments of the disclosed ethylene interpolymers. N.A.A. Elemental Density Melt Index Analysis (ppm) Sample Code (g/cm³) I₂ (dg/min) Ti Mg Cl Al Example 4 0.9154 0.97 9.6 287 45 140 Example 5 0.9163 1.04 6.7 261 70 131 Example 6 0.9152 0.67 5.2 245 48 119 Example 7 0.9155 0.70 7.7 365 102 177 Example 8 0.9176 4.64 7.6 234 86 117 Example 9 0.9190 0.91 6.4 199 78 99 Example 51 0.9165 1.01 5.9 207 73 106 Example 52 0.9169 0.85 5.2 229 104 112 Example 53 0.9164 0.90 7.3 347 101 167 Example 54 0.9176 0.94 7.5 295 100 146 Example 55 0.9170 0.91 7.1 189 101 90 Example 41 0.9178 0.93 7.2 199 103 92 Example 42 0.9176 0.99 7.5 188 104 86 Example 43 0.9174 1.08 7.4 192 101 91 Example 44 0.9179 0.93 7.2 230 121 110 Example 102 0.9176 0.97 9.5 239 60 117 Example 115 0.9171 0.75 5.1 258 115 130 Example 61 0.9396 4.82 8.3 352 96 179 Example 10 0.9168 0.94 7.8 333 91 170 Example 120 0.9204 1.00 7.3 284 75 149 Example 130 0.9232 0.94 5.8 292 114 147 Example 131 0.9242 0.95 8.6 81.4 173 94 Example 200 0.9250 1.04 6.3 90.1 190 104 

1-111. (canceled)
 112. A manufactured article comprising at least one layer comprising an ethylene interpolymer product comprising: (I) a first ethylene interpolymer; (II) a second ethylene interpolymer, and; (III) optionally a third ethylene interpolymer; wherein said first ethylene interpolymer is produced using a single site catalyst formulation comprising a component (i) defined by the formula (L^(A))_(a)M(Pl)_(b)(Q)_(n) wherein LA is selected from the group consisting of unsubstituted cyclopentadienyl, substituted cyclopentadienyl, unsubstituted indenyl, substituted indenyl, unsubstituted fluorenyl and substituted fluorenyl; M is a metal selected from the group consisting of titanium, hafnium and zirconium; Pl is a phosphinimine ligand; Q is independently selected from the group consisting of a hydrogen atom, a halogen atom, a C₁₋₁₀ hydrocarbyl radical, a C₁₋₁₀ alkoxy radical and a C₅₋₁₀ aryl oxide radical; wherein each of said hydrocarbyl, alkoxy, and aryl oxide radicals may be unsubstituted or further substituted by a halogen atom, a C₁₋₁₈ alkyl radical, a C₁₋₈ alkoxy radical, a C₆₋₁₀ aryl or aryloxy radical, an amido radical which is unsubstituted or substituted by up to two C₁₋₈ alkyl radicals or a phosphido radical which is unsubstituted or substituted by up to two C₁₋₈ alkyl radicals; wherein a is 1; b is 1; n is 1 or 2; and (a+b+n) is equivalent to the valence of the metal M; wherein said second ethylene interpolymer is produced using a first in-line Ziegler-Natta catalyst formulation; wherein said third ethylene interpolymer is produced using said first in-line Ziegler-Natta catalyst formulation or a second in-line Ziegler-Natta catalyst formulation, and; wherein said ethylene interpolymer product has a Dilution Index, Y_(d), greater than
 0. 113. The manufactured article of claim 112, wherein said single site catalyst formulation further comprises: an alumoxane co-catalyst; a boron ionic activator, and; optionally a hindered phenol.
 114. The manufactured article of claim 112, wherein said ethylene interpolymer product is further characterized as having one or more of: a) ≧0.03 terminal vinyl unsaturations per 100 carbon atoms; b) ≧3 parts per million (ppm) of a total catalytic metal; c) a Dimensionless Modulus, X_(d), greater than
 0. 115. The manufactured article of claim 112, wherein said ethylene interpolymer product has a melt index from about 0.4 to about 100 dg/minute; wherein melt index is measured according to ASTM D1238 (2.16 kg load and 190° C.).
 116. The manufactured article of claim 112, wherein said ethylene interpolymer product has a density from about 0.950 to about 0.970 g/cc; wherein density is measured according to ASTM D792.
 117. The manufactured article of claim 112, wherein said ethylene interpolymer product has a M_(w)/M_(n) from about 2 to about
 25. 118. The manufactured article of claim 112 having a CDBI₅₀ from about 55% to about 98%.
 119. The manufactured article of claim 112; wherein (I) said first ethylene interpolymer constitutes from about 15 to about 60 weight percent of said ethylene interpolymer product and has a melt index from about 0.01 to about 200 dg/min and a density from about 0.855 to about 0.975 g/cc; (II) said second ethylene interpolymer constitutes from about 30 to about 85 weight percent of said ethylene interpolymer product and has a melt index from about 0.3 to about 1000 dg/min and a density from about 0.89 to about 0.975 g/cc; (III) said third ethylene interpolymer constitutes from about 0 to about 30 weight percent of said ethylene interpolymer product and has a melt index from about 0.5 to about 2000 dg/min and a density from about 0.89 to about 0.975 g/cc; wherein weight percent is the weight of said first, said second or said third ethylene interpolymer, individually, divided by the weight of said ethylene interpolymer product; wherein melt index is measured according to ASTM D1238 (2.16 kg load and 190° C.), and; wherein density is measured according to ASTM D792.
 120. The manufactured article of claim 112; wherein said ethylene interpolymer product is synthesized using a solution polymerization process.
 121. The manufactured article of claim 112; wherein said ethylene interpolymer product further comprises from 0 to about 1 mole percent of one or more C₃ to C₁₀ α-olefins.
 122. The manufactured article of claim 112, wherein said ethylene interpolymer product has 1 part per million (ppm) of a metal A; wherein said metal A originates from said component (i).
 123. The manufactured article of claim 112, wherein said ethylene interpolymer product contains a metal B and optionally a metal C and the total amount of said metal B plus said metal C is from about 3 to about 11 parts per million; wherein said metal B originates from said first in-line Ziegler-Natta catalyst formulation and said metal C originates from said second in-line Ziegler-Natta catalyst formulation; optionally said metal B and said metal C are the same metal.
 124. The manufactured article of claim 123; wherein said metal B and said metal C, are independently selected from titanium, zirconium, hafnium, vanadium, niobium, tantalum, chromium, molybdenum, tungsten, manganese, technetium, rhenium, iron, ruthenium or osmium.
 125. The manufactured article of claim 112; wherein (I) said first ethylene interpolymer has a first CDBI₅₀ from about 70 to about 98%; (II) said second ethylene interpolymer has a second CDBI₅₀ from about 45 to about 98%, and; (III) said third ethylene interpolymer has a third CDBI₅₀ from about 35 to about 98%.
 126. The manufactured article of claim 125; wherein said first CDBI₅₀ is higher than said second CDBI₅₀ and said first CDBI₅₀ is higher than said third CDBI₅₀.
 127. The manufactured article of claim 112; wherein (I) said first ethylene interpolymer has a first M_(w)/M_(n) from about 1.7 to about 2.8; (II) said second-ethylene interpolymer has a second M_(w)/M_(n) from about 2.2 to about 4.4, and; (III) said third ethylene interpolymer has a third M_(w)/M_(n) from about 2.2 to about 5.0; wherein said first M_(w)/M_(n) is lower than said second M_(w)/M_(n) and said third M_(w)/M_(n).
 128. The manufactured article of claim 112; wherein said ethylene interpolymer product has a first AHO melt strength that is from about 5% to about 30% higher compared with a comparative ethylene interpolymer synthesized using one or more single-site catalyst formulations.
 129. The manufactured article of claim 112; wherein said manufactured article has a first heat deflection temperature that is from 4° C. to 10° C. higher compared with a control manufactured article having the same construction but said ethylene interpolymer product is replaced with a comparative ethylene interpolymer synthesized using one or more single-site catalyst formulations.
 130. The manufactured article of claim 112; wherein said manufactured article has a first half time of crystallization (t_(1/2)) that is at least 70% lower compared with a control manufactured article having the same construction but said ethylene interpolymer product is replaced with a comparative ethylene interpolymer synthesized using one or more single-site catalyst formulations.
 131. The manufactured article of claim 112; wherein said manufactured article is a film, a container or a lid. 